System for conversion of crude oil to petrochemicals and fuel products integrating steam cracking, fluid catalytic cracking, and conversion of naphtha into chemical rich reformate

ABSTRACT

Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking, fluid catalytic cracking and conversion of naphtha to chemical rich reformate. Feeds to the mixed feed steam cracker include light products from hydroprocessing zones within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline and FCC naphtha aromatics extraction zone within the battery limits. Chemical reformate from straight run naphtha streams is used as an additional feed to the aromatics extraction zone and or the mixed feed steam cracker.

RELATED APPLICATIONS

This application is a Continuation of U.S. patent application Ser. No.15/817,148 filed Nov. 17, 2017, which:

claims priority to U.S. Provisional Patent Application No. 62/424,883filed Nov. 21, 2016, U.S. Provisional Patent Application No. 62/450,018filed Jan. 24, 2017, and U.S. Provisional Patent Application No.62/450,060 filed Jan. 24, 2017; and

is a Continuation-In-Part of U.S. patent application Ser. No. 15/710,799filed Sep. 20, 2017, which claims priority to U.S. Provisional PatentApplication No. 62/424,883 filed Nov. 21, 2016, U.S. Provisional PatentApplication No. 62/450,018 filed Jan. 24, 2017, and U.S. ProvisionalPatent Application No. 62/450,058 filed Jan. 24, 2017, the contents ofwhich are all incorporated herein by reference in their entireties.

BACKGROUND OF THE INVENTION Field of the Invention

The inventions disclosed herein relate to an integrated process andsystem for converting crude oil to petrochemicals and fuel products.

Description of Related Art

The lower olefins (i.e., ethylene, propylene, butylene and butadiene)and aromatics (i.e., benzene, toluene and xylene) are basicintermediates which are widely used in the petrochemical and chemicalindustries. Thermal cracking, or steam pyrolysis, is a major type ofprocess for forming these materials, typically in the presence of steam,and in the absence of oxygen. Typical feedstocks for steam pyrolysis caninclude petroleum gases, such as ethane, and distillates such asnaphtha, kerosene and gas oil. The availability of these feedstocks isusually limited and requires costly and energy-intensive process stepsin a crude oil refinery.

A very significant portion of ethylene production relies on naphtha asthe feedstock. However, heavy naphtha has a lower paraffin and higheraromatics content than light naphtha, making it less suitable asfeedstock in the production of ethylene without upgrading. Heavy naphthacan vary in the amount of total paraffins and aromatics based on itssource. Paraffins content can range between about 27-70%, naphthenescontent can range between about 15-60%, and the aromatics content canrange between about 10-36% (volume basis).

Many chemicals producers are limited by the supply and quality of feedfrom nearby refiners due to reliance on oil refinery by-products asfeed. Chemicals producers are also limited by the high cost of oilrefining and its associated fuels markets, which may negativelyinfluence the economic value of refinery sourced feeds. Higher globalfuel efficiency standards for automobiles and trucks will reduce fuelsdemand and narrow refinery margins, and may complicate the economics offuels and chemicals supply and/or markets.

A need remains in the art for improved processes for converting crudeoil to basic chemical intermediates such as lower olefins and aromatics.In addition, a need remains in the art for new approaches that offerhigher value chemical production opportunities with greater leverage oneconomies of scale.

SUMMARY

In accordance with one or more embodiments, the invention relates to anintegrated process for producing petrochemicals and fuel product from acrude oil feed. The integrated process includes an initial separationstep to separate from a crude oil feed in an atmospheric distillationzone at least a fraction comprising straight run naphtha and lightercomponents, one or more middle distillate fractions, fractions, and anatmospheric residue fraction. A vacuum gas oil fraction is separatedfrom the atmospheric residue fraction in a vacuum distillation zone. Ina distillate hydroprocessing (“DHP”) zone, such as a dieselhydrotreater, at least a portion of the middle distillates are processedto produce at least a naphtha fraction and a diesel fuel fraction. Thevacuum gas oil fraction is processed in a fluid catalytic cracking zoneto produce at least a light olefins FCC fraction that is recovered aspetrochemicals, an FCC naphtha fraction and a cycle oil fraction.

The light components such as LPG from the atmospheric distillation zone,and an aromatics extraction zone raffinate, are processed in a mixedfeed steam cracking zone. All or a portion of the straight run naphthais passed to a catalytic reforming zone to produce chemical richreformate as additional feed to the aromatics extraction zone. Theproducts from the mixed feed steam cracking zone include a mixed productstream comprising H₂, methane, ethane, ethylene, mixed C3s and mixedC4s; a pyrolysis gasoline stream; and a pyrolysis oil stream.

From the mixed product stream C3s and the mixed C4s, petrochemicalsethylene, propylene and butylenes are recovered. Ethane and non-olefinicC3s are recycled to the mixed feed steam cracking zone, and non-olefinicC4s are recycled to the mixed feed steam cracking zone or to a separateprocessing zone for production of additional petrochemicals. Pyrolysisgasoline is treated in a py-gas hydroprocessing zone to producehydrotreated pyrolysis gasoline. The hydrotreated pyrolysis gasoline isrouted to the aromatics extraction zone to recover aromatic products andthe aromatics extraction zone raffinate that is recycled to the mixedfeed steam cracking zone.

Still other aspects, embodiments, and advantages of these exemplaryaspects and embodiments, are discussed in detail below. Moreover, it isto be understood that both the foregoing information and the followingdetailed description are merely illustrative examples of various aspectsand embodiments, and are intended to provide an overview or frameworkfor understanding the nature and character of the claimed aspects andembodiments. The accompanying drawings are included to provideillustration and a further understanding of the various aspects andembodiments, and are incorporated in and constitute a part of thisspecification. The drawings, together with the remainder of thespecification, serve to explain principles and operations of thedescribed and claimed aspects and embodiments.

BRIEF DESCRIPTION OF THE DRAWINGS

The invention will be described in further detail below and withreference to the attached drawings in which the same or similar elementsare referred to by the same number, and where:

FIG. 1 schematically depicts operations upstream of a steam crackercomplex in embodiments of processes for producing petrochemicals andfuel products integrating fluid catalytic cracking and steam cracking;

FIG. 2 schematically depicts operations upstream of a steam crackercomplex in further embodiments of processes for producing petrochemicalsand fuel products integrating fluid catalytic cracking and steamcracking;

FIG. 3 schematically depicts operations downstream of and including asteam cracker complex in embodiments of processes for producingpetrochemicals and fuel products integrating fluid catalytic crackingand steam cracking;

FIG. 4 schematically depicts operations downstream of and including asteam cracker complex in further embodiments of processes for producingpetrochemicals and fuel products integrating fluid catalytic crackingand steam cracking;

FIG. 5 schematically depicts operations downstream of and including asteam cracker complex in further embodiments of processes for producingpetrochemicals and fuel products integrating fluid catalytic crackingand steam cracking;

FIG. 6 schematically depicts operations downstream of and including asteam cracker complex in embodiments of processes for producingpetrochemicals and fuel products integrating fluid catalytic cracking,steam cracking and metathesis;

FIG. 7 schematically depicts operations downstream of and including asteam cracker complex in embodiments of processes for producingpetrochemicals and fuel products integrating fluid catalytic cracking,steam cracking and mixed butanol production;

FIG. 8 schematically depicts operations downstream of and including asteam cracker complex in embodiments of processes for producingpetrochemicals and fuel products integrating fluid catalytic cracking,steam cracking, metathesis and mixed butanol production;

FIGS. 9 and 10 schematically depict operations upstream of a steamcracker complex in further embodiments of processes for producingpetrochemicals and fuel products integrating fluid catalytic crackingand steam cracking;

FIG. 11 schematically depicts operations downstream of and including asteam cracker complex in further embodiments of processes for producingpetrochemicals and fuel products integrating fluid catalytic crackingand steam cracking;

FIGS. 12 and 13 schematically depict operations upstream of a steamcracker complex in additional embodiments of processes for producingpetrochemicals and fuel products integrating fluid catalytic crackingand steam cracking;

FIGS. 14, 15 and 16 schematically depict operation of a catalyticreforming zone for production of chemical rich reformate;

FIG. 17 schematically depicts operation of a catalytic reforming zone inanother embodiment;

FIG. 18 schematically depicts a single reactor hydrocracking zone;

FIG. 19 schematically depicts a series-flow hydrocracking zone withrecycle;

FIG. 20 schematically depicts a two-stage hydrocracking zone withrecycle;

FIG. 21 schematically depicts operations downstream of and including asteam cracker complex in additional embodiments of processes forproducing petrochemicals and fuel products integrating fluid catalyticcracking and steam cracking;

FIGS. 22 and 23 depict general operations of types of fluid catalyticcracking operations;

FIG. 24 schematically depicts operations downstream of and including asteam cracker complex in further embodiments of processes for producingpetrochemicals and fuel products integrating fluid catalytic cracking,steam cracking and metathesis;

FIG. 25 schematically depicts operations downstream of and including asteam cracker complex in further embodiments of processes for producingpetrochemicals and fuel products integrating fluid catalytic crackingand steam cracking; and

FIGS. 26 and 27 schematically depict operations upstream of a steamcracker complex in still further embodiments of processes for producingpetrochemicals and fuel products integrating fluid catalytic crackingand steam cracking.

DESCRIPTION

Process scheme configurations are disclosed that enable conversion ofcrude oil feeds with several processing units in an integrated mannerinto petrochemicals. The designs utilize minimum capital expenditures toprepare suitable feedstocks for the steam cracker complex. Theintegrated process for converting crude oil to petrochemical productsincluding olefins and aromatics, and fuel products, includes mixed feedsteam cracking, fluid catalytic cracking and conversion of naphtha tochemical rich reformate. Feeds to the mixed feed steam cracker includelight products from hydroprocessing zones within the battery limits,recycle streams from the C3 and C4 olefins recovery steps, and raffinatefrom a pyrolysis gasoline and FCC naphtha aromatics extraction zonewithin the battery limits. Chemical reformate from straight run naphthastreams is used as an additional feed to the aromatics extraction zoneand or the mixed feed steam cracker.

The phrase “a major portion” with respect to a particular stream orplural streams means at least about 50 wt % and up to 100 wt %, or thesame values of another specified unit.

The phrase “a significant portion” with respect to a particular streamor plural streams means at least about 75 wt % and up to 100 wt %, orthe same values of another specified unit.

The phrase “a substantial portion” with respect to a particular streamor plural streams means at least about 90, 95, 98 or 99 wt % and up to100 wt %, or the same values of another specified unit.

The phrase “a minor portion” with respect to a particular stream orplural streams means from about 1, 2, 4 or 10 wt %, up to about 20, 30,40 or 50 wt %, or the same values of another specified unit.

The term “crude oil” as used herein refers to petroleum extracted fromgeologic formations in its unrefined form. Crude oil suitable as thesource material for the processes herein include Arabian Heavy, ArabianLight, Arabian Extra Light, other Gulf crudes, Brent, North Sea crudes,North and West African crudes, Indonesian, Chinese crudes, or mixturesthereof. The crude petroleum mixtures can be whole range crude oil ortopped crude oil. As used herein, “crude oil” also refers to suchmixtures that have undergone some pre-treatment such as water-oilseparation; and/or gas-oil separation; and/or desalting; and/orstabilization. In certain embodiments, crude oil refers to any of suchmixtures having an API gravity (ASTM D287 standard), of greater than orequal to about 20°, 30°, 32°, 34°, 36°, 38°, 40°, 42° or 44°.

The acronym “AXL” as used herein refers to Arab Extra Light crude oil,characterized by an API gravity of greater than or equal to about 38°,40°, 42° or 44°, and in certain embodiments in the range of about38°-46°, 38°-44°, 38°-42°, 38°-40.5°, 39°-46°, 39°-44°, 39°-42° or39°-40.5°.

The acronym “AL” as used herein refers to Arab Light crude oil,characterized by an API gravity of greater than or equal to about 30°,32°, 34°, 36° or 38°, and in certain embodiments in the range of about30°-38°, 30°-36°, 30°-35°, 32°-38°, 32°-36°, 32°-35°, 33°-38°, 33°-36°or 33°-35°.

The acronym “LPG” as used herein refers to the well-known acronym forthe term “liquefied petroleum gas,” and generally is a mixture of C3-C4hydrocarbons. In certain embodiments, these are also referred to as“light ends.”

The term “naphtha” as used herein refers to hydrocarbons boiling in therange of about 20-205, 20-193, 20-190, 20-180, 20-170, 32-205, 32-193,32-190, 32-180, 32-170, 36-205, 36-193, 36-190, 36-180 or 36-170° C.

The term “light naphtha” as used herein refers to hydrocarbons boilingin the range of about 20-110, 20-100, 20-90, 20-88, 32-110, 32-100,32-90, 32-88, 36-110, 36-100, 36-90 or 36-88° C.

The term “heavy naphtha” as used herein refers to hydrocarbons boilingin the range of about 90-205, 90-193, 90-190, 90-180, 90-170, 93-205,93-193, 93-190, 93-180, 93-170, 100-205, 100-193, 100-190, 100-180,100-170, 110-205, 110-193, 110-190, 110-180 or 110-170° C.

In certain embodiments naphtha, light naphtha and/or heavy naphtha referto such petroleum fractions obtained by crude oil distillation, ordistillation of intermediate refinery processes as described herein.

The modifying term “straight run” is used herein having its well-knownmeaning, that is, describing fractions derived directly from theatmospheric distillation unit, optionally subjected to steam stripping,without other refinery treatment such as hydroprocessing, fluidcatalytic cracking or steam cracking. An example of this is “straightrun naphtha” and its acronym “SRN” which accordingly refers to “naphtha”defined above that is derived directly from the atmospheric distillationunit, optionally subjected to steam stripping, as is well known.

The term “kerosene” as used herein refers to hydrocarbons boiling in therange of about 170-280, 170-270, 170-260, 180-280, 180-270, 180-260,190-280, 190-270, 190-260, 193-280, 193-270 or 193-260° C.

The term “light kerosene” as used herein refers to hydrocarbons boilingin the range of about 170-250, 170-235, 170-230, 170-225, 180-250,180-235, 180-230, 180-225, 190-250, 190-235, 190-230 or 190-225° C.

The term “heavy kerosene” as used herein refers to hydrocarbons boilingin the range of about 225-280, 225-270, 225-260, 230-280, 230-270,230-260, 235-280, 235-270, 235-260 or 250-280° C.

The term “atmospheric gas oil” and its acronym “AGO” as used hereinrefer to hydrocarbons boiling in the range of about 250-370, 250-360,250-340, 250-320, 260-370, 260-360, 260-340, 260-320, 270-370, 270-360,270-340 or 270-320° C.

The term “heavy atmospheric gas oil” and its acronym “H-AGO” as usedherein in certain embodiments refer to the heaviest cut of hydrocarbonsin the AGO boiling range including the upper 3-30° C. range (e.g., forAGO having a range of about 250-360° C., the range of H-AGO includes aninitial boiling point from about 330-357° C. and an end boiling point ofabout 360° C.).

The term “medium atmospheric gas oil” and its acronym “M-AGO” as usedherein in certain embodiments in conjunction with H-AGO to refer to theremaining AGO after H-AGO is removed, that is, hydrocarbons in the AGOboiling range excluding the upper about 3-30° C. range (e.g., for AGOhaving a range of about 250-360° C., the range of M-AGO includes aninitial boiling point of about 250° C. and an end boiling point of fromabout 330-357° C.).

In certain embodiments, the term “diesel” is used with reference to astraight run fraction from the atmospheric distillation unit. Inembodiments in which this terminology is used, the diesel fractionrefers to medium AGO range hydrocarbons and in certain embodiments alsoin combination with heavy kerosene range hydrocarbons.

The term “atmospheric residue” and its acronym “AR” as used herein referto the bottom hydrocarbons having an initial boiling point correspondingto the end point of the AGO range hydrocarbons, and having an end pointbased on the characteristics of the crude oil feed.

The term “vacuum gas oil” and its acronym “VGO” as used herein refer tohydrocarbons boiling in the range of about 370-550, 370-540, 370-530,370-510, 400-550, 400-540, 400-530, 400-510, 420-550, 420-540, 420-530or 420-510° C.

The term “light vacuum gas oil” and its acronym “LVGO” as used hereinrefer to hydrocarbons boiling in the range of about 370-425, 370-415,370-405, 370-395, 380-425, 390-425 or 400-425° C.

The term “heavy vacuum gas oil” and its acronym “HVGO” as used hereinrefer to hydrocarbons boiling in the range of about 425-550, 425-540,425-530, 425-510, 450-550, 450-540, 450-530 or 450-510° C.

The term “vacuum residue” and its acronym “VR” as used herein refer tothe bottom hydrocarbons having an initial boiling point corresponding tothe end point of the VGO range hydrocarbons, and having an end pointbased on the characteristics of the crude oil feed.

The term “fuels” refers to crude oil-derived products used as energycarriers. Fuels commonly produced by oil refineries include, but are notlimited to, gasoline, jet fuel, diesel fuel, fuel oil and petroleumcoke. Unlike petrochemicals, which are a collection of well-definedcompounds, fuels typically are complex mixtures of different hydrocarboncompounds.

The terms “kerosene fuel” or “kerosene fuel products” refer to fuelproducts used as energy carriers, such as jet fuel or other kerosenerange fuel products (and precursors for producing such jet fuel or otherkerosene range fuel products). Kerosene fuel includes but is not limitedto kerosene fuel products meeting Jet A or Jet A-1 jet fuelspecifications.

The terms “diesel fuel” and “diesel fuel products” refer to fuelproducts used as energy carriers suitable for compression-ignitionengines (and precursors for producing such fuel products). Diesel fuelincludes but is not limited to ultra-low sulfur diesel compliant withEuro V diesel standards.

The term “aromatic hydrocarbons” or “aromatics” is very well known inthe art. Accordingly, the term “aromatic hydrocarbon” relates tocyclically conjugated hydrocarbons with a stability (due todelocalization) that is significantly greater than that of ahypothetical localized structure (e.g., Kekule structure). The mostcommon method for determining aromaticity of a given hydrocarbon is theobservation of diatropicity in its 1H NMR spectrum, for example thepresence of chemical shifts in the range of from 7.2 to 7.3 ppm forbenzene ring protons.

The terms “naphthenic hydrocarbons” or “naphthenes” or “cycloalkanes”are used herein having their established meanings and accordinglyrelates to types of alkanes that have one or more rings of carbon atomsin the chemical structure of their molecules.

The term “wild naphtha” is used herein to refer to naphtha productsderived from hydroprocessing units such as distillate hydroprocessingunits, diesel hydroprocessing units and/or gas oil hydroprocessingunits.

The term “unconverted oil” and its acronym “UCO,” is used herein havingits known meaning, and refers to a highly paraffinic fraction from ahydrocracker with a low nitrogen, sulfur and nickel content andincluding hydrocarbons having an initial boiling point corresponding tothe end point of the AGO range hydrocarbons, in certain embodiments theinitial boiling point in the range of about 340-370° C., for instanceabout 340, 360 or 370° C., and an end point in the range of about510-560° C., for instance about 540, 550 or 560° C. UCO is also known inthe industry by other synonyms including “hydrowax.”

The terms “reformate” or “chemical reformate” as used herein refer to amixture of hydrocarbons that are rich in aromatics, and are intermediateproducts in the production of chemicals and/or gasoline, and includehydrocarbons boiling in the range of about 30-200, 40-200, 30-185,40-185, 30-170 or 40-170° C.

The term “C # hydrocarbons” or “C #”, is used herein having itswell-known meaning, that is, wherein “#” is an integer value, and meanshydrocarbons having that value of carbon atoms. The term “C #+hydrocarbons” or “C #+” refers to hydrocarbons having that value or morecarbon atoms. The term “C #− hydrocarbons” or “C #−” refers tohydrocarbons having that value or less carbon atoms. Similarly, rangesare also set forth, for instance, C1-C3 means a mixture comprising C1,C2 and C3.

The term “petrochemicals” or “petrochemical products” refers to chemicalproducts derived from crude oil that are not used as fuels.Petrochemical products include olefins and aromatics that are used as abasic feedstock for producing chemicals and polymers. Typical olefinicpetrochemical products include, but are not limited to, ethylene,propylene, butadiene, butylene-1, isobutylene, isoprene, cyclopentadieneand styrene. Typical aromatic petrochemical products include, but arenot limited to, benzene, toluene, xylene, and ethyl benzene.

The term “olefin” is used herein having its well-known meaning, that is,unsaturated hydrocarbons containing at least one carbon-carbon doublebond. In plural, the term “olefins” means a mixture comprising two ormore unsaturated hydrocarbons containing at least one carbon-carbondouble bond. In certain embodiments, the term “olefins” relates to amixture comprising two or more of ethylene, propylene, butadiene,butylene-1, isobutylene, isoprene and cyclopentadiene.

The term “BTX” as used herein refers to the well-known acronym forbenzene, toluene and xylenes.

The term “make-up hydrogen” is used herein with reference tohydroprocessing zones to refer to hydrogen requirements of the zone thatexceed recycle from conventionally integrated separation vessels; incertain embodiments as used herein all or a portion of the make-uphydrogen in any given hydroprocessing zone or reactor within a zone isfrom gases derived from the steam cracking zone(s) and the reformingzone(s) in the integrated processes and systems.

The term “crude to chemicals conversion” as used herein refers toconversion of crude oil into petrochemicals including but not limited tolower olefins such as ethylene, propylene, butylenes (includingisobutylene), butadiene, MTBE, butanols, benzene, ethylbenzene, toluene,xylenes, and derivatives of the foregoing.

The term “crude to chemicals conversion ratio” as used herein refers tothe ratio, on a mass basis, of the influent crude oil before desalting,to petrochemicals.

The term “crude C4” refers to the mixed C4 effluent from a steamcracking zone.

The term “C4 Raffinate 1” or “C4 Raff-1” refers to the mixed C4s streamleaving the butadiene extraction unit, that is, mixed C4s from the crudeC4 except butadiene.

The term “C4 Raffinate 2” or “C4 Raff-2” refers to the mixed C4s streamleaving the MTBE unit, that is, mixed C4s from the crude C4 exceptbutadiene and isobutene.

The term “C4 Raffinate 3” or “C4 Raff-3” refers to the mixed C4s streamleaving the C4 distillation unit, that is, mixed C4s from the crude C4except butadiene, isobutene, and butane-1.

The terms “pyrolysis gasoline” and its abbreviated form “py-gas” areused herein having their well-known meaning, that is, thermal crackingproducts in the range of C5 to C9, for instance having an end boilingpoint of about 204.4° C. (400° F.), in certain embodiments up to about148.9° C. (300° F.).

The terms “pyrolysis oil” and its abbreviated form “py-oil” are usedherein having their well-known meaning, that is, a heavy oil fraction,C10+, that is derived from steam cracking.

The terms “light pyrolysis oil” and its acronym “LPO” as used herein incertain embodiments refer to pyrolysis oil having an end boiling pointof about 440, 450, 460 or 470° C.

The terms “heavy pyrolysis oil” and its acronym “HPO” as used herein incertain embodiments refer to pyrolysis oil having an initial boilingpoint of about 440, 450, 460 or 470° C.

The term “light cycle oil” and its acronym “LCO” as used herein refersto the light cycle oil produced by fluid catalytic cracking units. Thedistillation cut for this stream is, for example, in the range of about220-330° C. LCO is used sometimes in the diesel blends depending on thediesel specifications, or it can be utilized as a cutter to the fuel oiltanks for a reduction in the viscosity and sulfur contents.

The term “heavy cycle oil” and its acronym “HCO” as used herein refer tothe heavy cycle oil which is produced by fluid catalytic cracking units.The distillation cut for this stream is, for example, in the range ofabout 330-510° C. HCO is used sometimes in an oil flushing system withinthe process. Additionally, HCO is used to partially vaporize thedebutanizer bottoms and then is recycled back as a circulating reflux tothe main fractionator in the fluid catalytic cracking unit.

The term “cycle oil” is used herein to refer to a mixture of LCO andHCO.

In general, the integrated process for producing petrochemicals and fuelproducts from a crude oil feed includes an initial separation step toseparate from a crude oil feed in an atmospheric distillation zone atleast a first atmospheric distillation zone fraction comprising straightrun naphtha; a second atmospheric distillation zone fraction comprisingat least a portion of the middle distillates, and a third atmosphericdistillation zone fraction comprising atmospheric residue. A firstvacuum distillation zone fraction comprising vacuum gas oil is separatedfrom the third atmospheric distillation zone fraction in a vacuumdistillation zone. In a distillate hydroprocessing (“DHP”) zone, such asa diesel hydrotreater, at least a portion of the second atmosphericdistillation zone fraction is processed to produce at least a first DHPfraction and a second DHP fraction, wherein the first DHP fractioncomprises naphtha and the second DHP fraction is used for diesel fuelproduction The first vacuum distillation zone fraction is processed in afluid catalytic cracking zone to produce at least a first fluidcatalytic cracking fraction corresponding to light olefins, a portion ofwhich are recovered as petrochemicals, a second fluid catalytic crackingfraction corresponding to fluid catalytic cracking naphtha and a thirdfluid catalytic cracking fraction corresponding to cycle oil.

The light components such as LPG from the atmospheric distillation zone,and an aromatics extraction zone raffinate, are processed in a mixedfeed steam cracking zone. All or a portion of the straight run naphthais passed to a catalytic reforming zone to produce chemical richreformate as additional feed to the aromatics extraction zone. Theproducts from the mixed feed steam cracking zone include a mixed productstream containing H₂, methane, ethane, ethylene, mixed C3s, and mixedC4s, a pyrolysis gasoline stream and a pyrolysis oil stream.

From the mixed product stream, hydrogen gas, fuel gas, andpetrochemicals ethylene, propylene and butylenes are recovered. Ethaneand non-olefinic C3s and C4s are recovered, with ethane and non-olefinicC3s recycled to the steam cracking complex, and non-olefinic C4s arerecycled to the steam cracking complex or passed to a separateprocessing zone for production of additional petrochemicals such aspropylene and/or mixed butanol liquids. Pyrolysis gasoline is treated ina py-gas hydroprocessing zone to produce hydrotreated pyrolysis gasolinethat is routed to an aromatics extraction complex to recover aromaticpetrochemicals and a raffinate, including pyrolysis gasoline raffinatethat is recycled to the steam cracking complex. In certain embodiments,fluid catalytic cracking naphtha is also hydroprocessed and passed tothe aromatics extraction complex to produce additional aromaticpetrochemicals and additional raffinate that is routed to the steamcracking complex.

FIGS. 1, 2 and 3 schematically depict embodiments of processes andsystems for conversion of crude oil to petrochemicals and fuel products,including a mixed feed steam cracking zone, a chemical reforming zoneand a high olefinic fluid catalytic cracking (HOFCC) zone 700.Generally, FIGS. 1 and 2 show operations upstream of a mixed feed steamcracking zone (MFSC) 230 while FIG. 3 shows operations downstream of thecrude oil conversion zone and including the mixed feed steam crackingzone 230. The integrated processes and systems include a vacuum gas oilhydroprocessing zone, which can operate as a vacuum gas oil hydrocracker320 as shown in FIG. 1 or as a vacuum gas oil hydrotreater 300 as shownin FIG. 2.

With reference to FIGS. 1 and 2, a crude oil feed 102, in certainembodiments AXL or AL, is separated into fractions in a crude complex100 typically including an atmospheric distillation zone (CDU) 110, asaturated gas plant 150 and a vacuum distillation zone 160. The crudeoil feed 102, in certain embodiments having LPG and light naphtharemoved, is separated into fractions the atmospheric distillation zone110. As shown in FIG. 1, light products, for instance, lighthydrocarbons with fewer than six carbons, are passed to the mixed feedsteam cracking zone 230. In particular, C2-C4 hydrocarbons 152 includingethane, propane and butanes are separated from the light ends and LPG112 from the atmospheric distillation zone 110 via the saturated gasplant 150. Optionally, other light products are routed to the saturatedgas plant 150 shown in dashed lines as stream 156, such as light gasesfrom refinery units within the integrated system and in certainembodiments, light gases from outside of the battery limits. Off-gasesfrom the fluid catalytic cracking unit, after passing through anunsaturated gas plant, can be integrated with off-gases from thesaturated gas plant 150 for common handling of the fuel gases.

The separated C2-C4 hydrocarbons 152 are routed to the mixed feed steamcracking zone 230. Off-gases 154 from the saturated gas plant 150 andoff-gases 208 from the mixed feed steam cracking zone 230 are removedand recovered as is typically known, for instance to contribute to afuel gas (“FG”) system.

Straight run naphtha 136 from the atmospheric distillation zone 110 ispassed to a catalytic reforming zone 400 to produce chemical richreformate 426. In certain embodiments, all, a substantial portion or asignificant portion of the straight run naphtha 136 is routed to thecatalytic reforming zone 400. Remaining naphtha (if any) can be routedto the mixed feed steam cracking zone 230 (as shown in dashed lines)and/or added to a gasoline pool. In addition, in certain embodiments thestraight run naphtha stream 136 contains naphtha from other sources asdescribed herein and sometimes referred to as wild naphtha, forinstance, naphtha range hydrocarbons from one or more of the integrateddistillate, gas oil and/or residue hydroprocessing units.

Furthermore, in certain embodiments, an optional diverter, shown as avalve and a stream indicated in dashed lines, is used to bypass thecatalytic reforming zone 400 and route all or a portion of the straightrun naphtha (full range, light naphtha, or heavy naphtha) directly themixed feed steam cracking zone 230. In this manner, a producer can varythe quantity of feed to tailor the desired outputs. Accordingly, all ora portion of the straight run naphtha can be routed to the catalyticreforming zone 400, and the remainder (if any) is directed to the mixedfeed steam cracking zone 230. The quantity can be determined, forinstance, based upon demand for olefinic petrochemicals, demand foraromatic petrochemicals, demand for gasoline, and/or minimum ranges forwhich the unit is operated depending on design capacity.

Middle distillates are used to produce diesel and/or kerosene, andadditional feed to the mixed feed steam cracking zone 230. In theembodiments shown in FIGS. 1 and 2, at least three different middledistillate cuts are processed for production of fuel products andpetrochemicals (via the steam cracker). In one example using thearrangements shown in FIGS. 1 and 2, a first atmospheric distillationzone middle distillate fraction 116, in certain embodiments referred toa kerosene fraction, contains light kerosene range hydrocarbons, asecond atmospheric distillation zone middle distillate fraction 122, incertain embodiments referred as a diesel fraction, contains heavykerosene range hydrocarbons and medium AGO range hydrocarbons, and athird atmospheric distillation zone middle distillate fraction 126, incertain embodiments referred to as an atmospheric gas oil fraction,contains heavy AGO range hydrocarbons. In another example using thearrangements shown in FIGS. 1 and 2, a first middle distillate fraction116 contains kerosene range hydrocarbons, a second middle distillatefraction 122 contains medium AGO range hydrocarbons and a third middledistillate fraction 126 contains heavy AGO range hydrocarbons. Inanother example using the arrangements shown in FIGS. 1 and 2, a firstmiddle distillate fraction 116 contains light kerosene rangehydrocarbons and a portion of heavy kerosene range hydrocarbons, asecond middle distillate fraction 122 contains a portion of heavykerosene range hydrocarbons and a portion of medium AGO rangehydrocarbons and a third middle distillate fraction 126 contains aportion of medium AGO range hydrocarbons and heavy AGO rangehydrocarbons.

For example, a first middle distillate fraction 116 can be processed ina kerosene sweetening process 170 to produce kerosene fuel product 172,for instance, jet fuel compliant with Jet A or Jet A-1 specifications,and optionally other fuel products (not shown). In certain embodimentsherein, all or a portion of the first middle distillate fraction 116 isnot used for fuel production, but rather is used as a feed fordistillate hydroprocessing so as to produce additional feed for themixed feed steam cracking zone 230.

A second middle distillate fraction 122 is processed in a distillatehydroprocessing zone such as a diesel hydrotreating zone 180, to producewild naphtha 184 and a diesel fuel fraction 182, for instance, compliantwith Euro V diesel standards. In additional embodiments, all or aportion of the first middle distillate fraction 116 can be treated withthe second middle distillate fraction 122, as denoted by dashed lines.

In certain embodiments, all, a substantial portion, a significantportion or a major portion of the wild naphtha 184 is routed to themixed feed steam cracking zone 230 alone, or in combination with otherwild naphtha fractions from within the integrated process; any portionthat is not passed to the mixed feed steam cracking zone 230 can berouted to the crude complex 100 and/or directly to the catalyticreforming zone 400 and/or to a gasoline pool. In further embodiments,all, a substantial portion, a significant portion or a major portion ofthe wild naphtha 184 is passed to the crude complex 100, alone, or incombination with other wild naphtha fractions from within the integratedprocess; any portion that is not passed to the crude complex 100 can berouted to the mixed feed steam cracking zone 230 and/or directly to thecatalytic reforming zone 400 and/or to a gasoline pool. In additionalembodiments, all, a substantial portion, a significant portion or amajor portion of the wild naphtha 184 is passed to the catalyticreforming zone 400, alone, or in combination with other wild naphthafractions from within the integrated process; any portion that is notpassed to the catalytic reforming zone 400 can be routed to the mixedfeed steam cracking zone 230 and/or to the crude complex 100 and/or to agasoline pool. In embodiments in which wild naphtha 184 is routedthrough the crude complex 100, all or a portion of the liquefiedpetroleum gas produced in the vacuum gas oil hydroprocessing zone can bepassed with the wild naphtha.

In certain embodiments (as denoted by dashed lines), all, a substantialportion, a significant portion or a major portion of the third middledistillate fraction 126 is routed to the vacuum gas oil hydroprocessingzone in combination with the vacuum gas oil stream 162; any portion thatis not passed to the vacuum gas oil hydroprocessing zone can be routedto the high olefinic fluid catalytic cracking zone 700, bypassing thevacuum gas oil hydroprocessing zone. In further embodiments (as denotedby dashed lines), all, a substantial portion, a significant portion or amajor portion of the third middle distillate fraction 126 is routed tothe high olefinic fluid catalytic cracking zone 700, bypassing thevacuum gas oil hydroprocessing zone; any portion that is not passed tothe high olefinic fluid catalytic cracking zone 700 can be routed to thevacuum gas oil hydroprocessing zone.

An atmospheric residue fraction 114 from the atmospheric distillationzone 110 is further separated in the vacuum distillation zone 160.Vacuum gas oil 162 from the vacuum distillation zone 160 is routed tothe vacuum gas oil hydroprocessing zone. The heaviest fraction 168 fromthe vacuum distillation zone 160, vacuum residue, can be sent to a fueloil (“FO”) pool or optionally processed in a residue treatment zone 800,shown in dashed lines. In certain embodiments, a minor portion of theatmospheric residue fraction 114 can bypass the vacuum distillation zone160 (not shown) and is routed to the optional residue treating zone 800.

In certain embodiments, all, a substantial portion, a significantportion or a major portion of the vacuum gas oil 162 is routed to thevacuum gas oil hydroprocessing zone. Any portion that is nothydroprocessed can be routed to the high olefinic fluid catalyticcracking zone 700. As shown in FIG. 1, vacuum gas oil hydroprocessing isin a vacuum gas oil hydrocracking zone 320 that can operate under mild,moderate or severe hydrocracking conditions, and generally produces ahydrocracked naphtha fraction 326, a diesel fuel fraction 322, and anunconverted oil fraction 324. The diesel fuel fraction 322 is recoveredas fuel, for instance, compliant with Euro V diesel standards, and canbe combined with the diesel fuel fraction 182 from the dieselhydrotreating zone 180. As shown in FIG. 2, vacuum gas oilhydroprocessing is in a vacuum gas oil hydrotreating zone 300 that canoperate under mild, moderate or severe hydrotreating conditions, andgenerally produces a hydrotreated gas oil fraction 304, naphtha and somemiddle distillates. Naphtha range products can be separated fromproducts within the vacuum gas oil hydrotreating zone 300 as ahydrotreated naphtha stream 306. Alternatively, or in conjunction withthe hydrotreated naphtha stream 306, a cracked distillates stream 308containing hydrotreated distillates (and in certain embodiments naphtharange products) are routed to diesel hydrotreating zone 180 for furtherhydroprocessing and/or separation into diesel hydrotreating zone 180products.

In certain embodiments, all, a substantial portion, a significantportion or a major portion of the wild naphtha fraction from the vacuumgas oil hydroprocessing zone, streams 326 or 306, is routed to the mixedfeed steam cracking zone 230, alone, or in combination with other wildnaphtha fractions from within the integrated process; any portion thatis not passed to the mixed feed steam cracking zone 230 can be routed tothe crude complex 100 and/or directly to the catalytic reforming zone400 and/or to the gasoline pool. In further embodiments, all, asubstantial portion, a significant portion or a major portion of thewild naphtha fraction from the vacuum gas oil hydroprocessing zone ispassed to the crude complex 100, alone, or in combination with otherwild naphtha fractions from within the integrated process; any portionthat is not passed to the crude complex 100 can be routed to the mixedfeed steam cracking zone 230 and/directly to the catalytic reformingzone 400 and/or to the gasoline pool. In additional embodiments, all, asubstantial portion, a significant portion or a major portion of thewild naphtha fraction from the vacuum gas oil hydroprocessing zone ispassed to the catalytic reforming zone 400, alone, or in combinationwith other wild naphtha fractions from within the integrated process;any portion that is not passed to the catalytic reforming zone 400 canbe routed to the mixed feed steam cracking zone 230 and/or to the crudecomplex 100 and/or to the gasoline pool. In embodiments in which wildnaphtha from the vacuum gas oil hydroprocessing zone is routed throughthe crude complex 100, all or a portion of the liquefied petroleum gasproduced in the vacuum gas oil hydroprocessing zone can be passed withthe wild naphtha.

Heavy product from the vacuum gas oil hydroprocessing zone is routed tothe high olefinic fluid catalytic cracking zone 700. In the embodimentswith the vacuum gas oil hydrotreating zone 300, heavy product is thehydrotreated gas oil fraction 304 that contains the portion of thevacuum gas oil hydrotreater 300 effluent that is at or above the AGO,H-AGO or VGO boiling range. In the embodiments with the vacuum gas oilhydrocracking zone 320, heavy product is the unconverted oil fraction324. All, a substantial portion, a significant portion or a majorportion of heavy product from the vacuum gas oil hydroprocessing zone isrouted to high olefinic fluid catalytic cracking zone 700. The remainder(if any) can be passed to the optional vacuum residue treating zone 800and/or passed to the mixed feed steam cracking zone 230. Alternatively,any remainder can be recycled and further processed (cracked toextinction in VGO hydrocracking) and/or bled from the system and/orpassed to the optional residue treating zone 800.

The high olefinic fluid catalytic cracking zone 700 is configured toproduce light olefin product 704 and high olefinic fluid catalyticcracking naphtha 706. It should be appreciated that the light olefinproduct 704 can be recovered from the high olefinic fluid catalyticcracking zone 700 as is known, or recovered in combination with theolefins recovery zone 270 and/or the mixed feed steam cracking zone 230as described herein. Off-gases from the high olefinic fluid catalyticcracking zone 700 can be integrated with the fuel gas system. In certainembodiments (not shown in FIG. 1), certain gases, after treatment in anunsaturated gas plant, can be routed to the separation units associatedwith the mixed feed steam cracking zone 230, and/or LPGs can be routedto the mixed feed steam cracking zone 230. All, a substantial portion, asignificant portion or a major portion of the gases containing lightolefins (a C2− stream and a C3+ stream) are routed through theunsaturated gas plant. The remainder, if any, can be routed to the mixedfeed steam cracking zone 230 and/or the olefins recovery train 270.

In certain embodiments, all or a portion of the high olefinic fluidcatalytic cracking naphtha 706 can be processed as described below (andin conjunction with FIG. 3) in a naphtha hydrotreatment and recoverycenter 610/620, to increase the quantity of raffinate as additional feedto the mixed feed steam cracking zone 230. Any portion of the higholefinic fluid catalytic cracking naphtha 706 that is not routed to thenaphtha hydrotreatment and recovery center 610/620, shown in dashedlines, is hydrotreated and recovered for fuel production (not shown).For instance, in modalities in which the objective is maximumpetrochemical production, all, a substantial portion, a significantportion or a major portion of the fluid catalytic cracking naphtha 706is routed to the naphtha hydrotreatment and recovery center 610/620; theremainder, if any, is recovered for fuel production and incorporationinto a gasoline pool.

In additional embodiments, as shown in FIG. 4, all or a portion of thehigh olefinic fluid catalytic cracking naphtha 706 is hydrotreated andrecovered for fuel production and incorporation into a gasoline pool(not shown). Optionally, a portion of the high olefinic fluid catalyticcracking naphtha 706 that is not recovered for fuel production can beprocessed in the naphtha hydrotreatment and recovery center 610/620, asshown in dashed lines, to increase the quantity of raffinate asadditional feed to the mixed feed steam cracking zone 230.

In additional embodiments, as shown in FIG. 5, all or a portion of thehigh olefinic fluid catalytic cracking naphtha 706 is hydrotreated in afluid catalytic cracking naphtha hydrotreating zone 670, and thehydrotreated fluid catalytic cracking naphtha stream 672 is directlyrouted to the mixed feed steam cracking zone 230. Any portion of thehigh olefinic fluid catalytic cracking naphtha 706 that is not routed tothe to the mixed feed steam cracking zone 230, shown in dashed lines, isrecovered for fuel production (not shown). In this manner, components ofthe hydrotreated fluid catalytic cracking naphtha stream 672, that arenot cracked in the mixed feed steam cracking zone 230, includingaromatics, increase the pyrolysis gasoline 212 from the mixed feed steamcracking zone 230, which are routed to the py-gas hydrotreatment andrecovery center 600/620. In certain embodiments using the fluidcatalytic cracking naphtha hydrotreating zone 670, all, a substantialportion, a significant portion or a major portion of the hydrotreatedfluid catalytic cracking naphtha stream 672 is routed to the mixed feedsteam cracking zone 230; the remainder, if any, can be routed toaromatics extraction 620 and/or recovered for fuel production andincorporation into a gasoline pool and/or passed to the chemicalreforming zone 400. In additional embodiments using the fluid catalyticcracking naphtha hydrotreating zone 670, all, a substantial portion, asignificant portion or a major portion of the hydrotreated fluidcatalytic cracking naphtha stream 672 is routed to the chemicalreforming zone 400, the remainder, if any, can be routed to aromaticsextraction 620 and/or recovered for fuel production and incorporationinto a gasoline pool and/or passed to the mixed feed steam cracking zone230.

Other products from the high olefinic fluid catalytic cracking zone 700include cycle oil, such as light cycle oil 708 and heavy cycle oil 710.In certain optional embodiments, all or a portion of the light cycle oil708 is routed to the distillate hydroprocessing zone 180, therebyincreasing the yield of the diesel fuel fraction 182 and wild naphtha184 that is passed to the mixed feed steam cracking zone 230. In certainembodiments, all, a substantial portion, a significant portion or amajor portion of the light cycle oil 708 is passed to the distillatehydroprocessing zone 180, and any remaining portion can be routed to thevacuum gas oil processing zone. Heavy cycle oil stream 710 can be routedto a fuel oil pool or used as feedstock for production of carbon black.

With reference to FIG. 3, the mixed feed steam cracking zone 230, whichoperates as a high severity or low severity thermal cracking process,converts its feed primarily into ethylene 202, propylene 204, mixed C4s206, pyrolysis gasoline 212, pyrolysis oil 218, and off-gases 208 thatcan be passed to an integrated fuel gas system. Further, hydrogen 210 isrecovered from the cracked products and can be recycled to hydrogenusers within the complex limits. Not shown are the ethane and propanerecycle, which are typical in steam cracking operations, although it isappreciated that in certain embodiments all or a portion of the ethaneand propane can be diverted. In certain embodiments, all, a substantialportion, a significant portion or a major portion of ethane is recycledto the mixed feed steam cracking zone 230, and all, a substantialportion, a significant portion or a major portion of propane is mixedfeed steam cracking zone 230. In certain embodiments hydrogen for allhydrogen users in the integrated process and system is derived fromhydrogen 210 recovered from the cracked products, and no outsidehydrogen is required once the process has completed start-up and reachedequilibrium. In further embodiments excess hydrogen can be recovered.

For simplicity, operations in an olefins recovery train are not shown,but are well known and are considered part of the mixed feed steamcracking zone 230 as described herein with respect to FIGS. 3, 4, 5, 6,7, 8 and 11.

The mixed C4s stream 206 containing a mixture of C4s from the mixed feedsteam cracking zone 230, known as crude C4s, is routed to a butadieneextraction unit 500 to recover a high purity 1,3-butadiene product 502.A first raffinate 504 (“C4-Raff-1”) containing butanes and butenes ispassed to a selective hydrogenation unit (SHU) and methyl tertiary butylether (“MTBE”) unit, SHU and MTBE zone 510, where it is mixed with highpurity fresh methanol 512 from outside battery limits to produce MTBE514.

A second raffinate 516 (“C4 Raff-2”) from the SHU and MTBE zone 510 isrouted to a C4 distillation unit 520 for separation into a 1-buteneproduct stream 522 and an alkane stream 524 (a third raffinate“C4-Raff-3”) containing residual C4s, all, a substantial portion, asignificant portion or a major portion of which is recycled to the mixedfeed steam cracking zone 230 although it is appreciated that in certainembodiments all or a portion of the residual C4s can be diverted.Separation of the ethylene 202, propylene 204 and the mixed C4s stream206 occurs in a suitable arrangement of known separation steps forseparating steam cracking zone effluents, including compressionstage(s), depropanizer, debutanizer, demethanizer and deethanizer.

Pyrolysis gasoline 212 from the steam cracking zone 230 is fed to thenaphtha hydrotreatment and recovery center 610/620. In certainembodiments, select hydrocarbons having 5-12 carbons are recovered fromuntreated pyrolysis gasoline and high olefinic fluid catalytic crackingnaphtha (“FCCN”) 706, and the remainder is subsequently hydrotreated foraromatics recovery. In the naphtha hydrotreating unit 610, diolefins andolefins in the pyrolysis gasoline are saturated. All, a substantialportion or a significant portion of the pyrolysis gasoline 212 from thesteam cracking zone 230 is passed to the naphtha hydrotreatment andrecovery center 610/620.

As noted above, in certain embodiments, all or a portion of the fluidcatalytic cracking naphtha 706 is used as additional feed to the mixedfeed steam cracking zone 230 without the hydrotreating and aromaticseparation steps, without the aromatic separation step, or without thehydrotreating step. In further embodiments, all or a portion of thefluid catalytic cracking naphtha 706 is recovered and used for fuelproduction.

Hydrotreated pyrolysis gasoline and fluid catalytic cracking naphtha (incertain embodiments having C5s removed and recycled to the mixed feedsteam cracking zone 230 instead of or in conjunction with C5s from thearomatics extraction zone 620) are routed to the aromatics extractionzone 620. The naphtha hydrotreating zone 610 and the aromaticsextraction zone 620 high olefinic fluid catalytic are shown forsimplicity in a single schematic block 610/620 in FIGS. 3, 4, 5, 6, 7, 8and 11. The naphtha hydrotreating zone 610 operates to hydrotreatpyrolysis gasoline 212 prior to aromatics recovery. In certain optionalembodiments, fluid catalytic cracking naphtha 706 can also behydrotreated in a separate hydrotreating zone (shown, for instance, inFIGS. 5, 21 and 24), and routed to the aromatics extraction zone 620with the hydrotreated pyrolysis gasoline.

In an embodiment herein, chemical rich reformate 426 is to be routed asadditional feed to the aromatics extraction zone 620. The chemical richreformate 426 can bypass naphtha hydrotreating, since it has beentreated in the catalytic reforming zone 400, although in certainembodiments the chemical rich reformate 426 can pass with the pyrolysisgasoline and/or the FCC naphtha. In further embodiments, modes ofoperation are provided in which the chemical rich reformate 426 canserve as feed to the aromatics extraction zone 620 and/or as gasolineblending components. In this manner, a producer can vary the quantity offeed to tailor the desired outputs. Accordingly, 0-100% of the chemicalrich reformate 426 can be routed to the aromatics extraction zone 620,and the remainder (if any) is directed to a gasoline blending pool (notshown). The quantity can be determined, for instance, based upon demandfor aromatic petrochemicals, demand for gasoline, and/or minimum rangesfor which the unit is operated depending on design capacity.

The aromatics extraction zone 620 includes, for instance, one or moreextractive distillation units, and operates to separate the hydrotreatedpyrolysis gasoline and fluid catalytic cracking naphtha into anaromatics stream 622 containing high-purity benzene, toluene, xylenesand C9 aromatics, which are recovered for chemical markets. C5 raffinate644 and non-aromatics 646 (for instance, C6-C9) are recycled to themixed feed steam cracking zone 230. In certain embodiments, all, asubstantial portion or a significant portion of the C5 raffinate 644 andnon-aromatics 646 are passed to the mixed feed steam cracking zone 230.A heavy aromatics stream 642 (for instance, C10-C12) can be used as anaromatic solvent, an octane boosting additive or as a cutter stock intoa fuel oil pool. In certain embodiments ethylbenzene 628 can berecovered.

In certain embodiments, pyrolysis oil 218 can be blended into the fueloil pool. In additional embodiments, pyrolysis oil 218 can be fractioned(not shown) into light pyrolysis oil and heavy pyrolysis oil. Forinstance, light pyrolysis oil can be blended with the first middledistillate stream 116 and/or the second middle distillate stream 122,for processing to produce diesel fuel product and/or additional feed tothe mixed feed steam cracking zone 230. In further embodiments lightpyrolysis oil derived from pyrolysis oil 218 can be processed in thevacuum gas oil hydroprocessing zone. In additional embodiments, lightpyrolysis oil derived from pyrolysis oil 218 can be blended into thefuel oil pool. In further embodiments, light pyrolysis derived frompyrolysis oil 218 can be processed in the residue treating zone 800. Incertain embodiments, all, a substantial portion, a significant portionor a major portion of light pyrolysis oil can be passed to the dieselhydrotreating zone 180 and/or the vacuum gas oil hydroprocessing zone;any remainder can be blended into the fuel oil pool. Heavy pyrolysis oilcan be blended into the fuel oil pool, used as a carbon black feedstockand/or processed in the optional residue treating zone 800. In certainembodiments, all, a substantial portion, a significant portion or amajor portion of the pyrolysis oil 218 (light and heavy) can beprocessed in the optional residue treating zone 800.

FIG. 6 schematically depicts further embodiments of processes andsystems for conversion of crude oil to petrochemicals and fuel products,with metathesis conversion of C4 and C5 olefins to produce additionalpropylene. The process operates as described with respect to any of FIG.1, 2, 4 or 5 upstream of the steam cracking operations and with respectto the fluid catalytic cracking operations.

Downstream of the steam cracking operations, the butadiene extractiontrain can optionally operate in a manner similar to that in FIG. 3 shownas the stream 524 from a diverter (in dashed lines) from the C4distillation unit 520 directly to the mixed feed steam cracking zone230.

In a metathesis mode of operation, mixed C4 raffinate stream 532 (“C4Raff 3”) from the C4 distillation unit 520 and C5 raffinate 540 from thenaphtha hydrotreatment and recovery center 610/620 are routed to themetathesis unit 530 for metathesis conversion to additional propylene534. In certain embodiments, all, a substantial portion, a significantportion or a major portion of the cracked C5s from the py-gashydrotreater can be routed to the metathesis unit 530 prior to aromaticsextraction. As indicated, a portion 536 of the ethylene mixed feed steamcracking product 202 can be routed to the metathesis unit 530. Inadditional embodiments, ethylene for the metathesis unit 530 is suppliedfrom outside the complex limits, instead of or in addition to theportion 536 of the ethylene mixed feed steam cracking product.

Selective recovery of various alkene and diene pyrolysis chemicalshaving four carbons, and metathesis conversion to produce additionalpropylene, is achieved using a metathesis unit 530. A stream 538containing a mixture of mostly saturated C4/C5 from the metathesis unit530 is recycled to the mixed feed steam cracking zone 230.

As in FIG. 3, in the configuration of FIG. 6, pyrolysis gasoline 212from the steam cracking zone 230 is routed to the naphtha hydrotreatmentand recovery center 610/620 where select hydrocarbons having 5-12carbons can be recovered from untreated pyrolysis gasoline and fluidcatalytic cracking naphtha, and the remainder is subsequentlyhydrotreated for aromatics recovery. In a py-gas hydrotreating unit(“HTU”), diolefins and olefins in the pyrolysis gasoline are saturated.In the aromatics extraction step, aromatics are separated fromhydrotreated pyrolysis gasoline and fluid catalytic cracking naphtha.For instance, aromatic extraction can separate the hydrotreatedpyrolysis gasoline and fluid catalytic cracking naphtha into high-puritybenzene, toluene, xylenes and C9 aromatics. C6-C9 aromatics stream 622,BTX, is recovered for chemical markets, C6-C9 non-aromatics stream 646is recycled to the mixed feed steam cracking zone 230, and C10-C12products stream 642 may be used as an aromatic solvent or as an octaneboosting additive. In certain embodiments ethylbenzene 628 can berecovered. C5 raffinate is routed to the metathesis unit 530 as shown asstream 540, and/or recycled to the mixed feed steam cracking zone 230(as in the embodiment of FIG. 3) via stream 644, shown in dashed linesin FIG. 6.

In the configuration depicted in FIG. 6, an optional diverter is shown,indicated as a diverter and stream in dashed lines, to bypass themetathesis conversion process, to therefore divert all, a substantialportion, a significant portion or a major portion of the C4 Raff-3 524to the mixed feed steam cracking zone 230. In a metathesis mode, flowcan be directed to the metathesis conversion unit 530. In furtheralternative modes, flow of the C4 Raff-3 524 can be directed to themixed feed steam cracking zone 230 and the metathesis conversion unit530. In this manner, a producer can vary the quantity of feed to tailorthe desired outputs. Accordingly, 0-100% of the third C4 raffinatestream 524 can be routed to the metathesis conversion unit 530, and theremainder (if any) is directed to the mixed feed steam cracking zone230. The quantity can be determined, for instance, based upon demand forethylene, demand for propylene, and/or minimum ranges for which the unitis operated depending on design capacity.

FIG. 7 schematically depicts further embodiments of processes andsystems for conversion of crude oil to petrochemicals and fuel products.The process operates as described with respect to FIG. 1, 2, 4 or 5upstream of the steam cracking operations and with respect to the fluidcatalytic cracking operations. In this embodiment, an additional step isprovided to convert a mixture of butenes into mixed butanols suitable asa gasoline blending oxygenate and for octane enhancement. Suitableprocesses to convert a mixture of butenes into mixed butanols aredescribed in one or more of commonly owned patent publicationsUS20160115107A1, US20150225320A1, US20150148572A1, US20130104449A1,US20120245397A1 and commonly owned U.S. Pat. No. 9,447,346B2, U.S. Pat.No. 9,393,540B2, U.S. Pat. No. 9,187,388B2, U.S. Pat. No. 8,558,036B2,all of which are incorporated by reference herein in their entireties.In certain embodiments, a particularly effective conversion processknown as “SuperButol™” technology is integrated, which is a one-stepprocess that converts a mixture of butenes into mixed butanol liquids.

Downstream of the steam cracking operations, the butadiene extractiontrain can optionally operate in a manner similar to that in FIG. 3 shownas the stream 524 from a diverter (in dashed lines) from the C4distillation unit 520 directly to the mixed feed steam cracking zone230. A crude C4 processing center 550 is integrated for selectiverecovery of various alkene and diene pyrolysis chemicals having fourcarbons, and in certain processing arrangements hydrating a portion ofthose C4's in a butanol production unit (such as a “SuperButol™” unit)to produce high value fuel additives.

For instance, the mixed butanols production zone 550 operates to convertbutenes to butanols from undervalued refinery/petrochemical mixed olefinstreams. The butanols provide an alternative option for oxygenates ingasoline blends. The crude C4 processing center 550 includes theconversion reaction of butenes to butanols, for instance, in one or morehigh pressure catalytic reactors followed by gravity separation ofbutenes and butanols from water, and subsequent separation of thebutanols product from butenes by distillation. Process stages includebutenes and water make-up and recycle, butanol reaction, high pressureseparation, low pressure separation, debutenizer distillation (productcolumn) and an aqueous distillation column.

FIG. 7 depicts a stream 552 containing butenes from the C4 distillationstep routed to a crude C4 processing zone such as a butanol productionunit 550 to convert the mixture of butenes into mixed butanol liquids554. In certain embodiments, all, a substantial portion, a significantportion or a major portion of stream 552 is routed to the butanolproduction unit 550. Alkanes 556 are recycled to the mixed feed steamcracking zone 230.

As in FIGS. 1 and 3, in the configuration of FIG. 7, pyrolysis gasoline212 from the steam cracking zone 230 is routed to the naphthahydrotreatment and recovery center 610/620 where select hydrocarbonshaving 5-12 carbons can be recovered from untreated pyrolysis gasolineand fluid catalytic cracking naphtha, and the remainder is subsequentlyhydrotreated for aromatics recovery. C5s are recycled to the mixed feedsteam cracking zone 230. In a py-gas hydrotreating unit, diolefins andolefins in the pyrolysis gasoline are saturated. Hydrotreated pyrolysisgasoline from the py-gas hydrotreating unit is routed to aromaticsextraction. In the aromatics extraction step, aromatics are separatedfrom hydrotreated pyrolysis gasoline and fluid catalytic crackingnaphtha. For instance, aromatic extraction can separate the hydrotreatedpyrolysis gasoline and fluid catalytic cracking naphtha into high-puritybenzene, toluene, xylenes and C9 aromatics. C6-C9 aromatics stream 622can be recovered for chemical markets, C5 raffinate 644 andnon-aromatics 646 (for instance, C6-C9) can be recycled to the mixedfeed steam cracking zone 230, and heavy aromatic 642 (for instance,C10-C12) products can be used as an aromatic solvent or as an octaneboosting additive. In certain embodiments ethylbenzene 628 can berecovered.

In the configuration depicted in FIG. 7, an optional diverter is shown,indicated as a diverter and stream in dashed lines, to bypass theprocess for conversion of a mixture of butenes into mixed butanols, totherefore divert all, a substantial portion, a significant portion or amajor portion of the C4 Raff-3 524 to the mixed feed steam cracking zone230. In alternative modes, flow can be directed to the mixed butanolsproduction zone 550 for conversion of a mixture of butenes into mixedbutanols. In further alternative modes, flow of the C4 Raff-3 524 can bedirected to the mixed feed steam cracking zone 230 and the mixedbutanols production zone 550. In this manner, a producer can vary thequantity of feed to tailor the desired outputs. Accordingly, 0-100% ofthe third C4 raffinate stream 524 can be routed to mixed butanolsproduction zone 550, and the remainder (if any) is directed to the mixedfeed steam cracking zone 230. The quantity can be determined, forinstance, based upon demand for ethylene, demand for mixed butanols,and/or minimum ranges for which the unit is operated depending on designcapacity

FIG. 8 schematically depicts further embodiments of processes andsystems for conversion of crude oil to petrochemicals and fuel products.In this embodiment, additional step(s) of metathesis conversion of C4and C5 olefins to produce additional propylene, and/or conversion of amixture of butenes into mixed butanols suitable as a gasoline blendingoxygenate and for octane enhancement, are integrated. The processoperates as described with respect to any of FIG. 1, 2, 4 or 5 upstreamof the steam cracking operations and with respect to the fluid catalyticcracking operations.

Downstream of the steam cracking operations, the butadiene extractiontrain can optionally operate in a manner similar to that in FIG. 3 shownas the stream 524 from a diverter (in dashed lines) from the C4distillation unit 520 directly to the mixed feed steam cracking zone 230as an optional mode of operation. The configuration in FIG. 8 integratesselective recovery of various alkene and diene pyrolysis chemicalshaving four carbons, metathesis conversion to produce additionalpropylene, and/or conversion of a mixture of butenes into mixed butanolssuitable as a gasoline blending oxygenate and for octane enhancement.

FIG. 8 depicts a stream 552 containing butenes from the C4 distillationstep (“C4 Raff-3”) routed to a crude C4 processing zone such as abutanol production unit 550 for conversion of the mixture of butenesinto mixed butanol liquids 554. Alkanes 556 are recycled to the mixedfeed steam cracking zone 230. In addition, a portion 532 of the 2-butenerich raffinate-3 from the C4 distillation unit 520 is passed to ametathesis unit 530 for metathesis conversion to additional propylene534. As indicated, a portion 536 of the ethylene mixed feed steamcracking product can be routed to the metathesis unit 530. In additionalembodiments, ethylene for the metathesis unit 530 is supplied fromoutside the complex limits, instead of or in addition to the portion 536of the ethylene product 202. A stream 538, having a mixture of mostlysaturated C4/C5 from metathesis unit, is recycled to the mixed feedsteam cracking zone.

As in FIG. 3, in the configuration of FIG. 8, pyrolysis gasoline 212from the steam cracking zone 230 is routed to the naphtha hydrotreatmentand recovery center 610/620 where select hydrocarbons having 5-12carbons can be recovered from untreated pyrolysis gasoline and fluidcatalytic cracking naphtha, and the remainder is subsequentlyhydrotreated for aromatics recovery. In a py-gas hydrotreating unit,diolefins and olefins in the pyrolysis gasoline are saturated.Hydrotreated pyrolysis gasoline from the py-gas hydrotreating unit isrouted to aromatics extraction. In the aromatics extraction step,aromatics are separated from hydrotreated pyrolysis gasoline and fluidcatalytic cracking naphtha. For instance, aromatic extraction canseparate the hydrotreated pyrolysis gasoline and fluid catalyticcracking naphtha into high-purity benzene, toluene, xylenes and C9aromatics. C6-C9 aromatics stream 622, BTX, can be recovered forchemical markets, non-aromatics 646 (for instance, C6-C9) can berecycled to the mixed feed steam cracking zone 230, and heavy aromatics642 (for instance, C10-C12) products can be used as an aromatic solventor as an octane boosting additive. In certain embodiments ethylbenzene628 can be recovered. 540 can be routed to the metathesis unit 530 asshown, and/or optionally recycled to the mixed feed steam cracking asshown in dashed lines, stream 644. In certain embodiments (not shown),all or a portion of the cracked C5s from the py-gas hydrotreater can berouted to the metathesis unit 530 prior to aromatics extraction.

In the configuration depicted in FIG. 8, an optional diverter is shown,indicated as a diverter and stream in dashed lines, to bypass themetathesis conversion process and the process for conversion of amixture of butenes into mixed butanols, to therefore divert all, asubstantial portion, a significant portion or a major portion of the C4Raff-3 524 to the mixed feed steam cracking zone 230. An optional valvealso can be provided to direct flow of the C4 Raff-3 to one or both ofthe metathesis conversion unit 530 and/or the mixed butanols productionzone 550 for conversion of a mixture of butenes into mixed butanols. Infurther alternative modes, flow of the C4 Raff-3 524 can be directed toeach of the mixed feed steam cracking zone 230, the metathesisconversion unit 530 (as stream 532), and the mixed butanols productionzone 550 (as stream 552). In this manner, a producer can vary thequantity of feed to tailor the desired outputs. Accordingly, all, asubstantial portion, a significant portion or a major portion of thethird C4 raffinate stream can be routed to the metathesis conversionunit 530, and the remainder (if any) is directed to the mixed feed steamcracking zone 230 and/or the mixed butanols production zone 550. Incertain embodiments, all, a substantial portion, a significant portionor a major portion of the third C4 raffinate stream is routed to themetathesis conversion unit 530, and the remainder (if any) is directedto the mixed feed steam cracking zone 230. In further embodiments, all,a substantial portion, a significant portion or a major portion of thethird C4 raffinate stream is routed to the metathesis conversion unit530, and the remainder (if any) is directed to the mixed butanolsproduction zone 550 for production of mixed butanols. In furtherembodiments, all, a substantial portion, a significant portion or amajor portion of the third C4 raffinate stream is routed to the mixedbutanols production zone 550 for production of mixed butanols, and theremainder (if any) is directed to both the mixed feed steam crackingzone 230 and the metathesis conversion unit 530. In further embodiments,all, a substantial portion, a significant portion or a major portion ofthe third C4 raffinate stream is routed to the mixed butanols productionzone 550 for production of mixed butanols, and the remainder (if any) isdirected to the mixed feed steam cracking zone 230. In furtherembodiments, all, a substantial portion, a significant portion or amajor portion of the third C4 raffinate stream is routed to the mixedbutanols production zone 550 for production of mixed butanols, and theremainder (if any) is directed to the metathesis conversion unit 530.The quantity can be determined, for instance, based upon demand forethylene, demand for propylene, demand for mixed butanols, and/orminimum ranges for which the unit is operated depending on designcapacity.

FIGS. 9 and 11 schematically depict further embodiments of processes andsystems for conversion of crude oil to petrochemicals and fuel products.In the arrangement of FIGS. 9 and 11, a crude oil feed 102, in certainembodiments AXL or AL, is fed to an atmospheric distillation zone 110 ofa crude complex 100. All or a portion of straight run naphtha 136 ispassed to a catalytic reforming zone 400 to produce chemical richreformate 426. Lighter products 152 are routed to a mixed feed steamcracking zone 230. Middle distillate fractions 116 and 122 are used toproduce kerosene and diesel, and wild naphtha 184 as additional feed tothe mixed feed steam cracking zone 230. In certain embodiments (asdenoted by dashed lines), all or a portion of a third middle distillatefraction 126 is routed to a vacuum gas oil hydroprocessing zone, whichcan operate as a vacuum gas oil hydrocracker as shown in FIG. 9 or as avacuum gas oil hydrotreater as shown in FIG. 10. In certain embodiments(as denoted by dashed lines), all or a portion of the third middledistillate fraction 126 is routed to the high olefinic fluid catalyticcracking zone 700, bypassing the vacuum gas oil hydroprocessing zone. Inadditional embodiments the third middle distillate fraction 126 can bedivided between the vacuum gas oil hydroprocessing zone and the higholefinic fluid catalytic cracking zone 700.

The atmospheric residue fraction 114 is further distilled in a vacuumdistillation zone 160. VGO 162 from the vacuum distillation zone 160 isrouted to a vacuum gas oil hydroprocessing zone, which can operate as ahigh severity vacuum gas oil hydrotreater or a mild vacuum gas oilhydrocracker. The heaviest fraction 168 from the vacuum distillationzone 160, vacuum residue, can be sent to a fuel oil (“FO”) pool oroptionally processed in a residue treatment zone 800, shown in dashedlines.

As shown in FIG. 9, a vacuum gas oil hydrotreater 300 can operate undermild, moderate or severe hydrotreating conditions, and generallyproduces cracked products 308 and hydrotreated gas oil 304. Crackedproducts 308 from the vacuum gas oil hydrotreater 300 are routed to thediesel hydrotreating zone 180. Hydrotreated gas oil 304 from the vacuumgas oil hydrotreater 300 is routed to a high olefinic fluid catalyticcracking zone 700 configured to produce maximum light olefin product704. It should be appreciated that the light olefin product 704 can berecovered from the high olefinic fluid catalytic cracking zone 700 as isknown, or recovered in combination with the olefins recovery zone 270and/or the mixed feed steam cracking zone 230 as described herein. Thehydrotreated gas oil fraction 304 generally contains the portion of thevacuum gas oil hydrotreater 300 effluent that is at or above the AGO,H-AGO or VGO range.

In certain embodiments, as shown in FIG. 10, a vacuum gas oilhydrocracker 320 can operate under mild, moderate or severehydrocracking conditions, and generally produces a hydrocracked naphthaproduct 326, a diesel fuel fraction 322, and an unconverted oil fraction324. Hydrocracked naphtha 326 from the vacuum gas oil hydrocracker 320is routed to the mixed feed steam cracking zone 230. The unconverted oilfraction 324 is routed to the high olefinic fluid catalytic crackingzone 700. The diesel fuel fraction 322 is recovered as fuel, forinstance, compliant with Euro V diesel standards, and can be combinedwith the diesel fuel fraction 182 from the diesel hydrotreating zone180.

Further, an aromatics recovery center 620 is included, in whicharomatics are separated from pyrolysis gasoline 212 and hydrotreatedpyrolysis gasoline can be obtained. C6-C9 aromatics 622 are recoveredfor chemical markets, C6-C9 non-aromatics 646 are recycled to the mixedfeed steam cracking zone 230, and C10-C12 products 642 can be used as anaromatic solvent or used as gasoline blenders as an octane boostingadditive.

In certain embodiments, as shown in dashed lines, high olefinic fluidcatalytic cracking naphtha 706 is hydrotreated and fed to the aromaticsextraction, the light naphtha and middle naphtha are fed to the mixedfeed steam cracking zone 230. The C5 and C9 streams from the higholefinic fluid catalytic cracker can be recycled to the mixed feed steamcracking zone 230.

In a further embodiment, all or a portion of the high olefinic fluidcatalytic cracking naphtha 706 is used as a gasoline blendstock, ratherbeing used in its entirety as feed to the mixed feed steam crackingzone; any remainder of the of the high olefinic fluid catalytic crackingnaphtha 706 can be used as feed to the mixed feed steam cracking zone230.

In additional embodiments, all or a portion of pyrolysis oil 218 fromthe steam cracking zone 230 can be passed to a catalytic hydrogenaddition process, such as a residue hydrocracking or conditioningprocess In additional embodiments, pyrolysis oil 218 is split into lightand heavy fractions, whereby the light fraction is fed to the gas oilhydroprocessing zone and the heavy fraction is fed to the catalytichydrogen addition process, such as a residue hydrocracking orconditioning process.

In still further embodiments, all or a portion of the hydrotreated gasoil fraction or unconverted oil fraction from the gas oilhydroprocessing zone is passed to an isodewaxing unit and ahydrofinishing unit, for instance, to enable production of group IIIlube oils or lube oil feedstocks.

FIGS. 12, 13 and 21 schematically depict embodiments of processes andsystems for conversion of crude oil to petrochemicals and fuel productsincluding a mixed feed steam cracking zone and a high olefinic fluidcatalytic cracking zone 700. Generally, FIGS. 12 and 13 show operationsupstream of the mixed feed steam cracking zone 230 while FIG. 21 showsoperations downstream of and including the mixed feed steam crackingzone 230.

A crude oil feed 102 is passed to a crude complex 100. In the embodimentof FIGS. 12, 13 and 21, the crude complex 100 generally includes anatmospheric distillation zone 110, a saturated gas plant 150 and avacuum distillation zone 160. The atmospheric distillation unit is usedin well-known arrangements.

Intermediate streams obtained from the feed 102 via separation in thecrude complex 100 include: off-gas 154, obtained within the crudecomplex 100 via the saturated gas plant 150, and which is passed to afuel gas system; a light ends stream 152, obtained within the crudecomplex 100 via the saturated gas plant 150, and which is passed to themixed feed steam cracking zone 230; one or more straight run naphthastream(s), in this embodiment a light naphtha stream 138 and a heavynaphtha stream 140, with all or a portion of the light naphtha stream138 being passed to the mixed feed steam cracking zone 230, and all or aportion of the heavy naphtha stream 140 passed to a catalytic reformingzone 400 to produce chemical rich reformate 426; a first middledistillate stream 118, such as a light kerosene stream, that is passedto a kerosene sweetening zone 170, such as a mercaptan oxidation zone; asecond middle distillate stream 120, such as a heavy kerosene stream,that is passed to a diesel hydrotreating zone 180; a third middledistillate stream 128, such as a medium atmospheric gas oil stream, thatis passed to the diesel hydrotreating zone 180; a fourth middledistillate stream 130, such as a heavy atmospheric gas oil stream, thatis passed to a high olefinic fluid catalytic cracking zone 700(directly, or optionally through the vacuum gas oil hydrotreating zone300, as indicated by dashed lines); an atmospheric residue fraction 114that is passed to the vacuum distillation zone 160 of the crude complex100; a vacuum gas oil stream 162 from the vacuum distillation zone 160that is passed to the vacuum gas oil hydroprocessing zone; and a vacuumresidue 168 from the vacuum distillation zone 160, all or a portion ofwhich can optionally be passed to a residue treating zone 800, and/or toa fuel oil pool.

The intermediate streams from the crude complex 100 are used in anefficient manner in the integrated process and system herein. The lightends stream 152, and a portion of the straight run naphtha stream(s), inthis embodiment light naphtha 138, are routed to the mixed feed steamcracking zone 230 as feed for conversion into light olefins and othervaluable petrochemicals. In certain embodiments, all, a substantialportion or a significant portion of the light naphtha 138 is routed tothe mixed feed steam cracking zone 230, and the remainder (if any)passed to a catalytic reforming zone 400. All or a portion of the heavynaphtha 140 from the atmospheric distillation zone 110 is passed to thecatalytic reforming zone 400 to produce chemical rich reformate 426,which can be routed as additional feed to the aromatics extraction zone620 or used for gasoline blending. In certain embodiments, all, asubstantial portion or a significant portion of the heavy naphtha 140 isrouted to the catalytic reforming zone 400, and the remainder (if any)passed to the mixed feed steam cracking zone 230. Either or both of thestraight run naphtha streams, light naphtha 138 and heavy naphtha 140,can optionally be steam-stripped in a side stripper prior to routing tothe mixed feed steam cracking zone 230.

Components of the crude complex not shown but which are well-known caninclude feed/product and pump-around heat exchangers, crude chargeheaters, crude tower(s), product strippers, cooling systems, hot andcold overhead drum systems including re-contactors and off-gascompressors, and units for water washing of overhead condensing systems.The atmospheric distillation zone 110 can include well-known designfeatures. Furthermore, in certain embodiments, naphtha, kerosene andatmospheric gas oil products from the atmospheric distillation columnare steam-stripped in side strippers, and atmospheric residue issteam-stripped in a reduced-size can section inside the bottom of theatmospheric distillation column.

The feed to the atmospheric distillation zone 110 is primarily the crudefeed 102, although it shall be appreciated that wild naphtha, LPGs andoff-gas streams from the diesel hydrotreating zone 180; and in certainembodiments from the vacuum gas oil hydroprocessing step and/or anoptional residue treating zone, can be routed to the atmosphericdistillation zone 110 where they are fractionated before being passed tothe cracking complex. A desalting unit (not shown) is typically includedupstream of the distillation zone 110. A substantial amount of the waterrequired for desalting can be obtained from a sour water stripper withinthe integrated process and system.

The desalting unit refers to a well-known arrangement of vessels fordesalting of crude oil, and as used herein is operated to reduce thesalt content to a target level, for instance, to a level of less than orequal to about 10, 5, or 3 wppm. In certain embodiments two or moredesalters are included to achieve a target salt content of less than orequal to about 3 wppm.

In one embodiment of a crude complex 100 herein, feed 102 is preheatedbefore entering a desalting unit, for instance, to a temperature (° C.)in the range of about 105-165, 105-150, 105-145, 120-165, 120-150,120-145, 125-165, 125-150, 125-145, and in certain embodiments about135. Suitable desalters are designed to remove salt down to a typicallevel of about 0.00285 kg/m³ (1 lb/1000 bbl) in a single stage. Incertain embodiments, plural preheat and desalting trains are employed.The desalter operating pressure can be based on a pressure margin abovecrude and water mixture vapor pressure at desalter operating temperatureto ensure liquid phase operation, for instance in the range of about2.75-4.15, 2.75-3.80, 2.75-3.65, 3.10-4.15, 3.10-3.80, 3.10-3.65,3.25-4.15, 3.25-3.80, 3.25-3.65 and in certain embodiments about 3.45barg.

The atmospheric distillation zone 110 can employ fractionated productsand pumparounds to provide enough heat for desalting. In certainembodiments, the desalter operating temperature can be controlled by adiesel pumparound swing heat exchanger. In certain embodiments, desalterbrine preheats desalter make-up water in a spiral type heat exchanger tominimize fouling and achieve rundown cooling against cooling waterbefore the brine is routed to the wastewater system.

In certain embodiments, desalted crude is preheated before entering apreflash tower, to a temperature (° C.) in the range of about 180-201,185-196, or 189-192. The preflash tower removes LPG and light naphthafrom the crude before it enters the final preheat exchangers. Thepreflash tower minimizes the operating pressure of the preheat train tomaintain liquid phase operation at the crude furnace pass valves andalso reduces the requisite size of the main crude column.

In one example of a suitable crude distillation system, a crude furnacevaporizes materials at or below a certain cut point, for instance, at atemperature (° C.) in the range of about 350-370, 355-365 or 360 (680°F.), before the crude enters the flash zone of the crude tower. Thefurnace is designed for a suitable outlet temperature, for instance, ata temperature (° C.) in the range of about 338-362, 344-354 or 348.9(660° F.). Crude column flash zone conditions are at a temperature (°C.) in the range about 328-374, 328-355, 337-374, 327-355, or 346.1(655° F.), and a pressure (barg) in the range of about 1.35-1.70,1.35-1.60, 1.44-1.70, 1.44-1.60 or 1.52.

In certain embodiments the crude tower contains 59 trays and producessix cuts, with draw temperatures for each product as follows: lightnaphtha, 104.4° C. (220° F.) (overhead vapor); heavy naphtha, 160.6° C.(321° F.) (sidedraw); kerosene, 205° C. (401° F.) (sidedraw); diesel,261.7° C. (503° F.) (sidedraw); AGO, 322.2° C. (612° F.) (sidedraw);atmospheric residue, 340.6° C. (645° F.) (bottoms). The heavy naphthadraw includes a reboiled side stripper against diesel pumparound, and iscontrolled to a 185° C. (365° F.) D86 end point. The kerosene drawincludes a steam stripper at 14.54 kg/m³ (5.1 lb steam per bbl); thedraw rate is limited on the back end by freeze point. The diesel drawincludes a steam stripper at 14.54 kg/m³ (5.1 lb steam per bbl), andthis draw is controlled to a 360° C. (680° F.) D86 95% point. The AGOdraw includes a steam stripper at 14.82 kg/m³ (5.2 lb steam per bbl),which sets the overflash at 2 vol % on crude. The crude tower alsocontains 3 pumparounds for top, diesel, and AGO. Diesel pumparoundprovides heat to the heavy naphtha stripper reboiler and debutanizerreboiler along with controlling desalter operating temperature via swingheat. The bottoms stream of the atmospheric column is steam stripped at28.5 kg/m³ (10 lb steam/bbl).

The atmospheric residue stream 114 from the atmospheric distillationzone 110 is further distilled in the vacuum distillation zone 160, whichfractionates the atmospheric residue fraction 114 into light and heavyvacuum gas oil streams 162 which are fed to the VGO hydroprocessingzone, as well as a vacuum residue stream 168, 0-100 wt % of which can beoptionally routed to a residue treating zone 800; any portion notsubjected to processing in the residue treating zone 800 can be routed,for instance, to a fuel oil pool (such as a high sulfur fuel oil pool).The vacuum distillation zone 160 can include well-known design features,such as operation at reduced pressure levels (mm Hg absolute pressure),for instance, in the range of about 30-40, 32-36 or 34, which can bemaintained by steam ejectors or mechanical vacuum pumps. Vacuum bottomscan be quenched to minimize coking, for instance, via exchange againstcrude at a temperature (° C.) in the range of about 334-352, 334-371,338-352, 338-371 or 343.3 (650° F.). Vacuum distillation can beaccomplished in a single stage or in plural stages. In certainembodiments, the atmospheric residue fraction 114 is heated in a directfired furnace and charged to vacuum fractionator at a temperature (° C.)in the range of about 390-436, 390-446, 380-436, 380-446 or 400-425.

In one embodiment, the atmospheric residue is heated to a temperature (°C.) in the range of about 399-420, 399-430, 389-420, 389-430 or 409.4(769° F.) in the vacuum furnace to achieve flash zone conditions of atemperature (° C.) in the range of about 392-412, 392-422, 382-412,382-422 or 401.7 (755° F.) and pressure levels (mm Hg absolute pressure)in the range of about 30-40, 32-36 or 34. The vacuum column is designedfor a theoretical cut point temperature (° C.) in the range of about524-551, 524-565, 511-551, 511-565 or 537.8 (1000° F.), by removinglight VGO and heavy VGO from the vacuum residue. The overhead vacuumsystem can include two parallel trains of jet ejectors each includingthree jets. A common vacuum pump is used at the final stage. In oneembodiment, the vacuum tower is sized for a 0.35 C-Factor and about a14.68 lpm/m² (0.3 gpm/ft²) wetting rate at the bottom of the wash zone.Wash zone slop wax is recycled to the vacuum furnace to minimize fueloil production. Vacuum bottoms are quenched via exchange against crudeto minimize coking at a temperature (° C.) in the range of about334-352, 334-371, 338-352, 338-371 or 343.3° C. (650° F.).

The saturated gas plant 150 generally comprises a series of operationsincluding fractionation and in certain systems absorption andfractionation, as is well known, with an objective to process light endsto separate fuel gas range components from LPG range components suitableas a steam cracker cracking zone feedstock. The saturated gas plant 150includes off-gas compression and recontacting to maximize LPG recovery,LPG fractionation from light naphtha, and off-gas/LPG amine treatment.The light ends that are processed in one or more saturated gas plantswithin embodiments of the integrated system and process herein arederived from the crude distillation, such as light ends and LPG. Inaddition, other light products can optionally be routed to the saturatedgas plant 150, shown in dashed lines as stream 156, such as light gasesfrom refinery units within the integrated system, and in certainembodiments light gases from outside of the battery limits. Forinstance, stream 156 can contain off-gases and light ends from thediesel hydrotreating zone 180, the gas oil hydroprocessing zone, thepy-gas hydrotreating zone 600 and/or the residue treating zone 800. Theproducts from the saturated gas plant 150 include: an off-gas stream154, containing C1-C2 alkanes, that is passed to the fuel gas systemand/or the steam cracker complex; and a light ends stream 152,containing C2+, that is passed to the mixed feed steam cracking unit230.

In certain embodiments, a suitable saturated gas plant 150 includesamine and caustic washing of liquid feed, and amine treatment of vaporfeed, before subsequent steps. The crude tower overhead vapor iscompressed and recontacted with naphtha before entering an aminescrubber for H₂S removal and is then routed to the steam crackercomplex. Recontact naphtha is debutanized to remove LPGs which are aminewashed and routed to the steam cracker complex. The debutanized naphthais routed separately from the heavy naphtha to the steam crackercomplex. As is known, light naphtha absorbs C4 and heavier hydrocarbonsfrom the vapor as it travels upward through an absorber/debutanizer.Off-gas from the absorber/debutanizer is compressed and sent to arefinery fuel gas system. A debutanizer bottoms stream is sent to themixed feed steam cracker as an additional source of feed.

All, a substantial portion or a significant portion of the heavy naphtha140 from the atmospheric distillation zone 110 (and in certainembodiments all or a portion of the heavy naphtha 138, not shown) ispassed to a catalytic reforming zone 400 to produce chemical richreformate 426, which can be routed as additional feed to the aromaticsextraction zone 620 and/used for gasoline blending. The catalyticreforming zone 400 generally includes a naphtha hydrotreating zone and acatalytic reforming zone. In certain embodiments the catalytic reformingzone also includes a reformate splitter and/or a benzene saturationunit. Product from the naphtha hydrotreating zone includes LPG andgases, and hydrotreated naphtha product that is routed to a naphthareformer. The naphtha reformer converts hydrotreated naphtha to chemicalrich reformate, which is a significant source of aromatic bulk chemicalsfrom the aromatics extraction zone downstream of the steam crackingoperations. In certain embodiments, all or a portion of the chemicalrich reformate can be used in a conventional manner, that is, asgasoline blending components; any remainder can be used as feed to themixed feed steam cracker.

The reactions involved in catalytic reforming include hydrocracking,dehydrocyclization, dehydrogenation, isomerization, and to a lesserextent, demethylation and dealkylation. A particular hydrocarbon/naphthafeed molecule may undergo more than one category of reaction and/or mayform more than one product. The hydrocarbon/naphtha feed composition,the impurities present therein, and the desired products will determinesuch process parameters as choice of catalyst(s), process type, and thelike.

The reaction rate for conversion of naphthenes to aromatics favors lowpressure, but so does coke formation which deactivates the catalyst.Thus with lower operating pressure the aromatics yield increases, butcatalyst regeneration must be done more frequently. To maintain thedesired lower operating pressure and also address coke formation,different methodologies are known. The general types of catalyticreforming process configurations differ in the manner in which thereforming catalyst is regenerated for removal of coke formed duringreaction. Catalyst regeneration, which involves combusting thedetrimental coke in the presence of oxygen, includes a semi-regenerativeprocess, cyclic regeneration and continuous catalyst regeneration (CCR).Semi-regeneration is the simplest configuration, and the entire unit,including all reactors in the series is shutdown for catalystregeneration in all reactors. Cyclic configurations utilize anadditional “swing” reactor to permit one reactor at a time to be takenoff-line for regeneration while the others remain in service. Continuouscatalyst regeneration configurations, which are the most complex,provide for essentially uninterrupted operation by catalyst removal,regeneration and replacement. While continuous catalyst regenerationconfigurations include the ability to increase the severity of theoperating conditions due to higher catalyst activity, the associatedcapital investment is necessarily higher.

In certain embodiments, the straight run naphtha, or the heavy naphtha,is separated into a normal paraffin (n-paraffin) rich stream and anon-normal rich stream containing branched paraffins. This isaccomplished using a separation zone 402 (shown in dashed lines asoptional), which can be, for instance, based on technology commerciallyavailable from Honeywell UOP, US (MaxEne™). The n-paraffin rich streambypasses the catalytic reforming zone and is routed to the mixed feedsteam cracking zone 230, enabling an increase in the combined yield ofethylene and propylene. Processing of the n-paraffin rich stream in themixed feed steam cracking zone 230 can also reduce coking which canfacilitate increases in throughput or extended run times betweende-coking cycles. The stream rich in non-normal paraffins also hassignificant benefits when processed in the catalytic reformer, includingimproved selectivity and reduced coke formation on the catalyst, whichcan facilitate increases in throughput.

A schematic process flow diagram of a catalytic reforming zone 400 isshown in FIGS. 14 and 15, and in certain embodiments combined with theunits of FIG. 16. A naphtha hydrotreating zone 410 is integrated with acatalytic reforming reaction zone 414 for the processing of a straightrun naphtha stream 136 (FIG. 14) or a heavy naphtha stream 140 (FIG.15), to produce chemical rich reformate 426 for chemical recovery, as agasoline blend component, or both for chemical recovery and as agasoline blend component. In certain embodiments, all, a substantialportion, a significant portion or a major portion of the chemical richreformate 426 is passed to the aromatics extraction zone 620, and anyremainder can be blended in a gasoline pool.

The naphtha feed 136 or 140 (or in certain embodiments the stream richin non-normal paraffins from an optional separation zone 402) ishydrotreated in the naphtha hydrotreating zone 410 to produce ahydrotreated naphtha stream 412. In embodiments of FIG. 15 in which thefeed to the naphtha hydrotreating zone 410 is heavy naphtha stream 140,light naphtha 138 can be routed to the mixed feed steam cracking unit230. In further embodiments, the feed to the naphtha hydrotreating zone410 can also be a full range naphtha including light naphtha (forinstance, both the heavy naphtha stream 140 combined with which can bethe light naphtha stream 138 described in other embodiments).Accordingly, depending on demand and/or the desired product slate, lightnaphtha 138 can be routed to the mixed feed steam cracking unit 230 toincrease production of olefinic petrochemicals, or alternativelyincluded with the feed to the catalytic reforming zone to increaseproduction of aromatic petrochemicals and/or fuel blending components.In certain embodiments, all, a substantial portion or a significantportion of light naphtha 138 is routed to the mixed feed steam crackingunit 230 (with any remainder optionally passed to the catalyticreforming zone 400); and all, a substantial portion or a significantportion of heavy naphtha 140 is routed to the catalytic reforming zone400 (with any remainder optionally passed to the mixed feed steamcracking unit 230).

Hydrotreating occurs in the presence of an effective amount of hydrogenobtained from recycle within the naphtha hydrotreating zone 410 (notshown), recycle reformer hydrogen 406, and if necessary make-up hydrogen408 (shown in dashed lines). Effluent off-gases are recovered from thenaphtha hydrotreating zone 410 and are passed the olefins recoverytrain, the saturated gas plant as part of the other gases stream 156,and/or directly to a fuel gas system. Liquefied petroleum gas isrecovered from the naphtha hydrotreating zone 410 and is routed to themixed feed steam cracking zone, the olefins recovery train and/or thesaturated gas plant.

In certain embodiments, all or a portion of any necessary make-uphydrogen 408 is derived from the steam cracker hydrogen stream 210 fromthe olefins recovery train 270. In additional embodiments hydrogen gasrecovered from the catalytic reforming reaction zone 414 providessufficient hydrogen to maintain the hydrogen requirements of naphthahydrotreating zone 410 when the reactions reach equilibrium. In furtherembodiments, there is a net hydrogen gain in the catalytic reformingzone so that hydrogen can be added, for instance, to the other hydrogenusers in the integrated process, and/or to the fuel gas that is used tooperate the various heating units within the integrated process. Asuitable naphtha hydrotreating zone 410 can include, but is not limitedto, systems based on technology commercially available from HoneywellUOP, US; Chevron Lummus Global LLC (CLG), US; Axens, IFP GroupTechnologies, FR; Shell Global Solutions, US, Haldor Topsoe A/S, DK; GTCTechnology US, LLC, US; or Exxon Mobil Corporation, US.

The naphtha hydrotreating zone 410 is operated under conditions, andutilizes catalyst(s), effective for removal of a significant amount ofthe sulfur and other known contaminants. Accordingly, the naphthahydrotreating zone 410 subjects feed to hydrotreating conditions toproduce a hydrotreated straight run naphtha stream 412 effective as feedto the catalytic reforming reaction zone 414. The naphtha hydrotreatingzone 410 operates under conditions of, e.g., temperature, pressure,hydrogen partial pressure, liquid hourly space velocity (LHSV), catalystselection/loading that are effective to remove at least enough sulfur,nitrogen, olefins and other contaminants needed to meet requisiteproduct specifications. For instance, hydrotreating in conventionalnaphtha reforming systems generally occurs under relatively mildconditions that are effective to remove sulfur and nitrogen to less than0.5 ppmw levels.

In certain embodiments, the naphtha hydrotreating zone 410 operatingconditions include:

a reactor inlet temperature (° C.) in the range of from about 355-400,355-375, 355-385, 370-400 or 360-390;

a reactor outlet temperature (° C.) in the range of from about 400-450,400-430, 410-450, 420-450 or 410-430;

a start of run (SOR) reaction temperature (° C.), as a weighted averagebed temperature (WABT), in the range of from about 330-375, 330-360,340-375, 355-375 or 330-350;

an end of run (EOR) reaction temperature (° C.), as a WABT, in the rangeof from about 390-435, 390-420, 390-410, 400-410 or 400-435;

a reaction inlet pressure (barg) in the range of from about 48-60,48-52, 48-55, 50-55 or 50-60;

a reaction outlet pressure (barg) in the range of from about 40-51,40-44, 40-48, 45-51 or 45-48;

a hydrogen partial pressure (barg) (outlet) in the range of from about24-34, 24-30, 27-34 27-30 or 27-32;

a hydrogen treat gas feed rate (SLt/Lt) up to about 645, 620, 570, 500or 530, in certain embodiments from about 413-640, 413-570, 413-542,465-620, 465-570, 465-542, 491-620, 491-570 or 491-542;

a quench gas feed (SLt/Lt) up to about 99, 90, 85, 78 or 70, in certainembodiments from about 57-90, 57-78, 57-75, 64-85, 64-78, 64-75, 68-85,68-78 or 68-75; and;

a make-up hydrogen feed rate (SLt/Lt) up to about 125, 110 or 102, incertain embodiments from about 78-120, 78-110, 78-102, 87-120, 87-110,87-102, 92-120, 92-110, 92-102 or 95-100.

Effective straight run naphtha reactor catalyst include those possessinghydrotreating functionality and which generally contain one or moreactive metal component of metals or metal compounds (oxides or sulfides)selected from the Periodic Table of the Elements IUPAC Groups 6-10. Incertain embodiments, the active metal component is one or more ofcobalt, nickel, tungsten and molybdenum. The active metal component istypically deposited or otherwise incorporated on a support, such asamorphous alumina, amorphous silica alumina, zeolites, or combinationsthereof. The catalyst used in the hydrotreating zone 410 can include oneor more catalyst selected from cobalt/molybdenum, nickel/molybdenum,nickel/tungsten, and cobalt/nickel/molybdenum. Combinations of one ormore of cobalt/molybdenum, nickel/molybdenum, nickel/tungsten andcobalt/nickel/molybdenum, can also be used. The combinations can becomposed of different particles containing a single active metalspecies, or particles containing multiple active species. In certainembodiments, cobalt/molybdenum hydrodesulfurization catalyst issuitable. Effective liquid hourly space velocity values (h⁻¹), on afresh feed basis relative to the hydrotreating catalysts, are in therange of from about 0.1-10.0, 0.1-5.0, 0.1-2.0, 0.3-10.0, 0.3-5.0,0.3-2.0, 0.5-10.0, 0.5-5.0, 0.5-2.0 or 0.8-1.2. Suitable hydrotreatingcatalysts used in the hydrotreating zone 410 have an expected lifetimein the range of about 28-44, 34-44, 28-38 or 34-38 months.

The hydrotreated naphtha stream is treated in the catalytic reformingzone to produce a reformate. A suitable catalytic reforming zone caninclude, but is not limited to, systems based on technology commerciallyavailable from Honeywell UOP, US; Chevron Lummus Global LLC (CLG), US;Axens, IFP Group Technologies, FR; Haldor Topsoe A/S, DK; or Exxon MobilCorporation, US.

The hydrotreated naphtha stream 412 is passed to a catalytic reformingreaction zone 414. In certain embodiments, all, a substantial portion ora significant portion of the hydrotreated naphtha stream 412 is passedto a catalytic reforming reaction zone 414, and any remainder can beblended in a gasoline pool. The reactor effluent 416, containing hotreformate and hydrogen, is cooled and passed to separator 418 forrecovery of hydrogen stream 404 and a separator bottoms stream 420. Thehydrogen stream 404 is split into a portion 406 which is compressed andrecycled back to the reformer reactors, and in certain embodiments anexcess hydrogen stream 428. The separator bottoms stream 420 is passedto a stabilizer column 422 to produce a light end stream 424 and areformate stream 426. The light end stream 424 is recovered and can berouted to the mixed feed steam cracking zone, the olefins recovery trainand/or the saturated gas plant.

The net hydrogen stream 428 can be recovered from the catalyticreforming reaction zone 414 (shown in dashed lines as optional), whichcomprises excess hydrogen passed to other hydrogen users including:those within the catalytic reforming zone 400 such as the naphthahydrotreating zone 410 and in certain embodiments a benzene saturationunit 438 shown in FIG. 16; and/or those elsewhere in the integratedprocess, such as the hydroprocessing unit(s) for middle distillates,pyrolysis gasoline, vacuum gas oil and/or transalkylation A suitablebenzene saturation system can include, but is not limited to, systemsbased on technology commercially available from Honeywell UOP, US;Axens, IFP Group Technologies, FR; or GTC Technology US, LLC, US.

In general, the operating conditions for the reactor(s) in the catalyticreforming reaction zone 414 include:

a reactor inlet temperature (° C.) in the range of from about 450-580,450-530, 450-500, 490-530 or 490-570;

a reactor outlet temperature (° C.) in the range of from about 415-540,415-490, 415-500, 440-500 or 450-530;

a start of run (SOR) reaction temperature (° C.), as a weighted averagebed temperature (WABT), in the range of from about 445-520, 445-480,445-500, 470-500 or 470-520;

an end of run (EOR) reaction temperature (° C.), as a WABT, in the rangeof from about 490-550, 490-510, 490-540; 500-550 or 520-540;

a reaction inlet pressure (barg) in the range of from about 1.5-50 or1.5-20;

a reaction outlet pressure (barg) in the range of from about 1.0-49 or1-20;

a hydrogen to hydrocarbon molar ratio in the range of from about2:1-5:1.

Cyclic and CCR process designs include online catalyst regeneration orreplacement, and accordingly the lower pressure ranges as indicatedabove are suitable. For instance, CCRs can operate in the range of about5 bar, while semi regenerative systems operate at the higher end of theabove ranges, with cyclic designs typically operating at a pressurehigher than CCRs and lower than semi regenerative systems.

An effective quantity of reforming catalyst is provided. Such catalystinclude mono-functional or bi-functional reforming catalyst whichgenerally contain one or more active metal component of metals or metalcompounds (oxides or sulfides) selected from the Periodic Table of theElements IUPAC Groups 8-10. A bi-functional catalyst has both metalsites and acidic sites. In certain embodiments, the active metalcomponent can include one or more of platinum, rhenium, gold, palladium,germanium, nickel, silver, tin, iridium or halides. The active metalcomponent is typically deposited or otherwise incorporated on a support,such as amorphous alumina, amorphous silica alumina, zeolites, orcombinations thereof. In certain embodiments, platinum or platinum alloysupported on alumina or silica or silica-alumina are the reformingcatalyst. Effective liquid hourly space velocity values (h⁻¹), on afresh feed basis relative to the hydrotreating catalysts, are in therange of from about 0.5-4, 0.5-2, 0.5-3, 1-3, 1-4, 1-2, 1.5-4 or 1.5-3.Suitable reforming catalysts used in the reforming reaction zone 414have an expected lifetime in the range of about 6-18, 12-26, 18-54 or24-72 months.

In certain embodiments, and with reference to FIG. 16, to increaseproduction of gasoline fuel components, the reformate stream is passedto separation and hydrogenation steps to reduce the total benzenecontent. For instance, instead of passing all or a portion of the totalreformate stream 426 to the aromatics extraction zone, it is passed to areformate splitter 430 and separated into one or more relativelybenzene-rich fractions 434 and one or more relatively benzene-leanfractions 432 and 436. Typically, the relatively benzene-rich middlefraction 434, known as a “benzene heart cut,” comprises about 10-20 vol% of the total reformate and contains about 20-30 vol % benzene. Incontrast, the relatively benzene-lean heavy reformate bottom fraction436 comprises about 40-80 V % of the total reformate and has a benzenecontent generally in the range of from about 0.3-1 vol %, which issufficiently low to be passed to a gasoline pool 444 without furtherprocessing. The light reformate top fraction 432 which includes about10-25 vol % of the total reformate, contains about 5-30 vol % benzeneand is recovered or blended with other product pools.

The heart cut fraction 434, which contains a majority of the benzenecontent of total reformate stream 426, can be passed to a hydrogenationunit 438, also referred to as a benzene saturation unit, or directly tothe aromatics extraction unit. Hydrogenation reactions occur in thepresence of a predetermined amount of hydrogen gas 440 for conversionreactions including conversion of benzene to cyclohexane, and for theproduction of a benzene-lean and in certain embodiments an essentiallybenzene-free, gasoline blending component 442.

All or a portion of the benzene-lean blending component 442 can be mixedwith the remaining gasoline pool constituents including the benzene-leanheavy reformate bottom fraction 436. For instance, when blended with theheavy reformate fraction 432 which can contain up to 1 vol % benzene, afinal gasoline product can be recovered which contains less than about 1vol % benzene. Further, all or a portion of benzene-lean blendingcomponent 442 can be routed to the mixed feed steam cracking zone 230.All of a portion of the light benzene lean fraction 432 can be routed toa gasoline pool or to the mixed feed steam cracking zone 230. All or aportion of the heavy benzene lean fraction 436 can be routed to thearomatics extraction zone 620 or to a gasoline pool.

In certain embodiments to maximize production of petrochemicals: all, asubstantial portion, a significant portion or a major portion of thebenzene-lean heavy reformate bottom fraction 436 is passed to thearomatics extraction zone, and any remainder can be passed to thegasoline pool; all, a substantial portion, a significant portion or amajor portion of light reformate top fraction 432 is passed to the mixedfeed steam cracking zone 230, and any remainder can be passed to thegasoline pool; and all, a substantial portion, a significant portion ora major portion of the benzene-lean blending component 442 can be routedto the mixed feed steam cracking zone 230, and any remainder can bepassed to the gasoline pool.

A typical gasoline blending pool includes C4 and heavier hydrocarbonshaving boiling points of less than about 205° C. In the catalyticreforming process, paraffins and naphthenes are restructured to produceisomerized paraffins and aromatics of relatively higher octane numbers.The catalytic reforming converts low octane n-paraffins to i-paraffinsand naphthenes. Naphthenes are converted to higher octane aromatics. Thearomatics are left essentially unchanged or some may be hydrogenated toform naphthenes due to reverse reactions taking place in the presence ofhydrogen.

In certain embodiments, the hydrogenation unit 438 operating conditionsinclude a reaction temperature (° C.) in the range of from about200-600, 225-600, 250-600, 400-600, 200-550, 225-550, 250-550 or400-550; and a reaction pressure (barg) in the range of from about 5-50,15-50, 20-50, 5-45, 15-45, 20-45, 30-50, 30-45 or 30-50. Thehydrogenation unit 438 is known, and can include but is not limited tosystems be based on technology commercially available from HoneywellUOP, US; Axens, IFP Group Technologies, FR; or GTC Technology US, LLC,US.

An effective quantity of catalyst having a suitable level of activematerials possessing hydrogenation functionality is provided in thebenzene saturation unit 438. Such catalyst generally contain one or moreactive metal component of metals or metal oxides, selected from thePeriodic Table of the Elements IUPAC Groups 6-10. In certainembodiments, the active metal component is one or more of nickel andplatinum. The active metal component is typically deposited or otherwiseincorporated on a support, such as amorphous alumina, amorphous silicaalumina, zeolites, or combinations thereof. Effective liquid hourlyspace velocity values (h⁻¹), on a fresh feed basis relative to thebenzene saturation unit catalysts, are in the range of from about0.1-10.0, 0.1-5.0, 0.1-2.0, 0.3-10.0, 0.3-5.0, 0.3-2.0, 0.5-10.0,0.5-5.0, 0.5-2.0 or 0.8-1.2. Suitable hydrotreating catalysts used inthe benzene saturation unit 438 have an expected lifetime in the rangeof about 28-44, 34-44, 28-38 or 34-38 months.

Referring to FIG. 17, another embodiment of a catalytic reforming system414 is schematically depicted. A series of reactors 414 are provided. Afeedstock, hydrotreated naphtha 412, is heat exchanged with a hotreformate stream 416 to increase the temperature of the feed. The heatedfeedstock is treated in a series of reaction zones containing reformerreactors 414, shown in the exemplary embodiment as zones A-D, althoughfewer or more zones can be used. The hot reformate stream 416 containshot product hydrogen and reformate.

The reforming reactions are endothermic resulting in the cooling ofreactants and products, requiring heating of effluent, typically bydirect-fired furnaces 446, prior to charging as feed to a subsequentreforming reactor 414. As a result of the very high reactiontemperatures, catalyst particles are deactivated by the formation ofcoke on the catalyst which reduces the available surface area and activesites for contacting the reactants.

Hot product hydrogen and reformate stream 416 passes through the heatexchanger and then to separator 418 for recovery of hydrogen stream 404and a separator bottoms stream 420. Recovered hydrogen stream 404 issplit with a portion compressed and recycled back to the reformerreactors, and excess hydrogen 428. The separator bottoms stream 420 issent to a stabilizer column 422 to produce a light end stream 424 and areformate stream 426.

As shown, the first middle distillate stream 118 is processed in akerosene sweetening zone 170, to remove unwanted sulfur compounds, as iswell-known. Treated kerosene is recovered as a kerosene fuel product172, for instance, jet fuel compliant with Jet A or Jet A-1specifications, and optionally other fuel products. In certainembodiments herein, all or a portion of the first middle distillatefraction 116 is not used for fuel production, but rather is used as afeed for distillate hydroprocessing so as to produce additional feed forthe mixed feed steam cracking zone 230.

For instance, a suitable kerosene sweetening zone 170 can include, butis not limited to, systems based on Merox™ technology (Honeywell UOP,US), Sweetn'K technology (Axens, IFP Group Technologies, FR) or Thiolex™technology (Merichem Company, US). Processes of these types arewell-established commercially and appropriate operating conditions arewell known to produce kerosene fuel product 172 and disulfide oils asby-product. In certain kerosene sweetening technologies impregnatedcarbon is utilized as catalyst to promote conversion to disulfide oil.In certain embodiments, common treatment of sour water from the kerosenesweetening zone 170 and other unit operations is employed to maximizeprocess integration.

For example, one arrangement of a kerosene sweetening zone includescaustic wash of the kerosene feed for residual H₂S removal, employing anelectrostatic coalescer (for instance using 10 degrees Baumé). Thereactor vessel containing an effective quantity of activated carboncatalyst utilizes air in conjunction with the caustic solution to affectthe oxidation of mercaptan to disulfides. Caustic is separated fromtreated kerosene in the bottom section of the reactor. After waterwashing, kerosene product passes upwards through one of two parallelsalt filters to remove free water and some soluble water. The keroseneproduct passes downward through one of two parallel clay filters forremoval of solids, moisture, emulsions and surfactants, to ensure thatthe kerosene product meets haze, color stability and water separationspecifications, for instance, compliant with Jet A specifications.

The second middle distillate stream 120 and the third middle distillatestream 128 are processed in a diesel hydrotreating zone 180 in thepresence of an effective amount of hydrogen obtained from recycle withinthe diesel hydrotreating zone 180 and make-up hydrogen 186. In certainembodiments, all or a portion of the make-up hydrogen 186 is derivedfrom a steam cracker product hydrogen 210 stream from the olefinsrecovery train 270. A suitable hydrotreating zone 180 can include, butis not limited to, systems based on technology commercially availablefrom Honeywell UOP, US; Chevron Lummus Global LLC (CLG), US; Axens, IFPGroup Technologies, FR; Haldor Topsoe A/S, DK; or joint technology fromKBR, Inc, US, and Shell Global Solutions, US.

The diesel hydrotreating zone 180 operates under conditions effectivefor removal of a significant amount of the sulfur and other knowncontaminants, for instance, to meet necessary sulfur specifications fora diesel fuel product 182, for instance, diesel fuel compliant with EuroV diesel standards. In addition, the hydrotreated naphtha fraction 184(sometimes referred to as wild naphtha) is recovered from the dieselhydrotreating zone 180, which is routed to the mixed feed steam crackingzone 230 as one of plural steam cracking feed sources. Effluentoff-gases are recovered from the diesel hydrotreating zone 180 and arepassed to the olefins recovery train, the saturated gas plant as part ofthe other gases stream 156, and/or directly to a fuel gas system.Liquefied petroleum gas can be recovered from the diesel hydrotreatingzone 180 and routed to the mixed feed steam cracking zone, the olefinsrecovery train and/or the saturated gas plant. In certain embodiments,the hydrotreated naphtha fraction 184 is routed through the crudecomplex 100, alone, or in combination with other wild naphtha fractionsfrom within the integrated process. In embodiments in which hydrotreatednaphtha fraction 184 is routed through the crude complex 100, all or aportion of the liquefied petroleum gas produced in the dieselhydrotreating zone 180 can be passed with the hydrotreated naphthafraction 184. In certain embodiments, all, a substantial portion or asignificant portion of the wild naphtha 184 is routed to the mixed feedsteam cracking zone 230 (directly or through the crude complex 100).

The diesel hydrotreating zone 180 can optionally process other fractionsfrom within the complex (not shown). In embodiments in which a kerosenesweetening zone 170 is used, all or a portion of the disulfide oil canbe additional feed to the diesel hydrotreating zone 180. Further, all ora portion of the first middle distillate fraction 116 can be additionalfeed to the diesel hydrotreating zone 180. Additionally, all or aportion of distillates from the vacuum gas oil hydroprocessing zone,and/or all or a portion of distillates from the optional vacuum residuetreatment zone, can be routed to the diesel hydrotreating zone 180. Anyportion of distillates not routed to the diesel hydrotreating zone 180can be passed to the crude complex 100 or routed to the mixed feed steamcracking zone 230. Further, all or a portion of light pyrolysis oil canbe routed to the diesel hydrotreating zone 180.

In certain embodiments, the diesel hydrotreating zone 180 also processesat least a portion of the light cycle oil 708 from the high olefinicfluid catalytic cracking zone 700. Any portion of the light cycle oil708 not routed to the diesel hydrotreating zone 180 can optionally bepassed to a fuel oil pool and/or processed in the integrated gas oilhydroprocessing zone. For example, no more than 0-30, 0-25, 0-20, 5-30,5-25, 5-20, 10-30, 10-25, or 10-20 wt % of the total light cycle oil 708from the high olefinic fluid catalytic cracking zone 700 can be routedto the diesel hydrotreating zone 180.

The diesel hydrotreating zone 180 can contain one or more fixed-bed,ebullated-bed, slurry-bed, moving bed, continuous stirred tank (CSTR) ortubular reactors, in series and/or parallel arrangement. In certainembodiments, the diesel hydrotreating zone 180 contains a layered bedreactor with three catalyst beds and having inter-bed quench gas, andemploys a layered catalyst system with the layer of hydrodewaxingcatalyst positioned between beds of hydrotreating catalyst. Additionalequipment, including exchangers, furnaces, feed pumps, quench pumps, andcompressors to feed the reactor(s) and maintain proper operatingconditions, are well known and are considered part of the dieselhydrotreating zone 180. In addition, equipment, including pumps,compressors, high temperature separation vessels, low temperatureseparation vessels and the like to separate reaction products andprovide hydrogen recycle within the diesel hydrotreating zone 180, arewell known and are considered part of the diesel hydrotreating zone 180.

In certain embodiments, the diesel hydrotreating zone 180 operatingconditions include:

a reactor inlet temperature (° C.) in the range of from about 296-453,296-414, 296-395, 336-453, 336-414, 336-395, 355-453, 355-414, 355-395or 370-380;

a reactor outlet temperature (° C.) in the range of from about 319-487,319-445, 319-424, 361-487, 361-445, 361-424, 382-487, 382-445, 382-424or 400-406;

a start of run (SOR) reaction temperature (° C.), as a weighted averagebed temperature (WABT), in the range of from about 271-416, 271-379,271-361, 307-416, 307-379, 307-361, 325-416, 325-379, 325-361 or340-346;

an end of run (EOR) reaction temperature (° C.), as a WABT, in the rangeof from about 311-476, 311-434, 311-414, 352-476, 352-434, 352-414,373-476, 373-434, 373-414 or 390-396;

a reaction inlet pressure (barg) in the range of from about 48-72,48-66, 48-63, 54-72, 54-66, 54-63, 57-72, 57-66 or 57-63;

a reaction outlet pressure (barg) in the range of from about 44-66,44-60, 44-58, 49-66, 49-60, 49-58, 52-66, 52-60 or 52-58;

a hydrogen partial pressure (barg) (outlet) in the range of from about32-48, 32-44, 32-42, 36-48, 36-44, 36-42, 38-48, 38-44 or 38-42;

a hydrogen treat gas feed rate (standard liters per liter of hydrocarbonfeed, SLt/Lt) up to about 400, 385, 353 or 337, in certain embodimentsfrom about 256-385, 256-353, 256-337, 289-385, 289-353, 289-337,305-385, 305-353 or 305-337;

-   -   a hydrogen quench gas feed rate (SLt/Lt) up to about 100, 85, 78        or 75, in certain embodiments from about 57-85, 57-78, 57-75,        64-85, 64-78, 64-75, 68-85, 68-78, or 68-75; and

a make-up hydrogen feed rate (SLt/Lt) up to about 110, 108, 100 or 95,in certain embodiments from about 70-108, 70-100, 70-95, 80-108, 80-100,80-95, 85-108, 85-100 or 85-95.

An effective quantity of hydrotreating catalyst is provided in thediesel hydrotreating zone 180, including those possessing hydrotreatingfunctionality and which generally contain one or more active metalcomponent of metals or metal compounds (oxides or sulfides) selectedfrom the Periodic Table of the Elements IUPAC Groups 6-10. In certainembodiments, the active metal component is one or more of Co, Ni, W andMo. The active metal component is typically deposited or otherwiseincorporated on a support, such as amorphous alumina, amorphous silicaalumina, zeolites, or combinations thereof. The catalyst used in thediesel hydrotreating zone 180 can include one or more catalyst selectedfrom Co/Mo, Ni/Mo, Ni/W, and Co/Ni/Mo. Combinations of one or more ofCo/Mo, Ni/Mo, Ni/W and Co/Ni/Mo, can also be used. The combinations canbe composed of different particles containing a single active metalspecies, or particles containing multiple active species. In certainembodiments, Co/Mo hydrodesulfurization catalyst is suitable. Effectiveliquid hourly space velocity values (h⁻¹), on a fresh feed basisrelative to the hydrotreating catalysts, are in the range of from about0.1-10.0, 0.1-5.0, 0.1-2.0, 0.3-10.0, 0.3-5.0, 0.3-2.0, 0.5-10.0,0.5-5.0, 0.5-2.0 or 0.8-1.2. Suitable hydrotreating catalysts used inthe diesel hydrotreating zone 180 have an expected lifetime in the rangeof about 28-44, 34-44, 28-38 or 34-38 months.

In certain embodiments, an effective quantity of hydrodewaxing catalystis also added. In such embodiments, effective hydrodewaxing catalystsinclude those typically used for isomerizing and cracking paraffinichydrocarbon feeds to improve cold flow properties, such as catalystscomprising Ni, W, or molecular sieves or combinations thereof. Catalystcomprising Ni/W, zeolite with medium or large pore sizes, or acombination thereof are suitable, along with catalyst comprisingaluminosilicate molecular sieves such as zeolites with medium or largepore sizes. Effective commercial zeolites include for instance ZSM-5,ZSM-11, ZSM-12, ZSM-22, ZSM-23, ZSM 35, and zeolites of type beta and Y.Hydrodewaxing catalyst is typically supported on an oxide support suchas Al₂O₃, SiO₂, ZrO₂, zeolites, zeolite-alumina, alumina-silica,alumina-silica-zeolite, activated carbon, and mixtures thereof.Effective liquid hourly space velocity values (h⁻¹), on a fresh feedbasis relative to the hydrodewaxing catalyst, are in the range of fromabout 0.1-12.0, 0.1-8.0, 0.1-4.0, 0.5-12.0, 0.5-8.0, 0.5-4.0, 1.0-12.0,1.0-8.0, 1.0-4.0 or 1.6-2.4. Suitable hydrodewaxing catalysts used inthe diesel hydrotreating zone 180 have an expected lifetime in the rangeof about 28-44, 34-44, 28-38 or 34-38 months.

In high capacity operations, two or more parallel trains of reactors areutilized. In such embodiments, the flow in the diesel hydrotreating zone180 is split after the feed pump into parallel trains, wherein eachtrain contains feed/effluent heat exchangers, feed heater, a reactor andthe hot separator. Each reactor contains three catalyst beds withinter-bed quench gas. A layered catalyst system is used with the layerof hydrodewaxing catalyst positioned between beds of hydrotreatingcatalyst. The trains recombine after the hot separators. Tops from thehot separators are combined and passed to a cold separator. Bottoms fromthe hot separators and from the cold separator are passed to a productstripper to produce stabilized ultra low sulfur diesel and wild naphtha.Tops from the cold separator are subjected to absorption and aminescrubbing. Recycle hydrogen is recovered, and passed (along with make-uphydrogen) to the reaction zone as treat gas and quench gas.

VGO 162 from the vacuum distillation zone 160 (or separate LVGO and HVGOfractions) is/are processed in a gas oil hydroprocessing zone 300 (FIG.12]) or 320 (FIG. 13]) in the presence of an effective amount ofhydrogen obtained from recycle within the gas oil hydroprocessing zoneand make-up hydrogen 302. In certain embodiments, all or a portion ofthe make-up hydrogen 302 is derived from the steam cracker hydrogenstream 210 from the olefins recovery train 270. In certain embodiments(not shown in FIGS. 12 and 13), all or a portion of the heavy middledistillate fraction, such as the third middle distillate fraction 126,e.g., atmospheric gas oil from the atmospheric distillation zone 110,can also be treated in the gas oil hydroprocessing zone, for instance, afull range AGO, or a fraction thereof such as a fourth middle distillatestream 130, such as heavy atmospheric gas oil. Further, a portion of thethird middle distillate fraction 126 can be routed to the gas oilhydroprocessing zone, while the remainder is routed to high olefinicfluid catalytic cracking zone 700, without passing through the vacuumgas oil hydroprocessing zone.

In accordance with the process herein, the severity of the gas oilhydroprocessing operation can be used to moderate the relative yield ofolefin and aromatic chemicals from the overall complex and improve theeconomic threshold of cracking heavy feeds. This application of a gasoil hydroprocessing zone. as a chemical yield control mechanism, isuncommon in the industry, where fuels products are typically the productobjectives.

In a hydrotreating mode of operation, as shown in FIG. 12, a vacuum gasoil hydrotreating zone 300 operates under suitable hydrotreatingconditions, and generally produces off-gas and light ends (not shown), awild naphtha stream 306 and hydrotreated gas oil 304. Effluent off-gasesare recovered from the gas oil hydrotreating zone 300 and are passed tothe olefins recovery train, the saturated gas plant as part of the othergases stream 156, and/or directly to a fuel gas system. Liquefiedpetroleum gas can be recovered from the gas oil hydrotreating zone 300and routed to the mixed feed steam cracking zone, the olefins recoverytrain and/or the saturated gas plant. The naphtha fraction 306 is routedto the mixed feed steam cracking zone 230. In certain embodiments, thehydrotreated naphtha fraction 306 is routed through the crude complex100, alone, or in combination with other wild naphtha fractions fromwithin the integrated process. In embodiments in which hydrotreatednaphtha fraction 306 is routed through the crude complex 100, all or aportion of the liquefied petroleum gas produced in the gas oilhydrotreating zone 300 can be passed with the hydrotreated naphthafraction 306. Hydrotreated gas oil 304 is routed to the high olefinicfluid catalytic cracking zone 700. In certain embodiments, as shown inFIG. 10 described below, in addition to or in conjunction with thehydrotreated naphtha fraction 306, all or a portion of the hydrotreateddistillates and naphtha from the gas oil hydrotreating zone 300 arepassed to the diesel hydrotreating zone 180.

The gas oil hydrotreating zone 300 generally operates under conditionseffective for removal of a significant amount of the sulfur and otherknown contaminants, and for conversion of the VGO 162 feed into a majorproportion of hydrotreated gas oil 304 that is passed to the higholefinic fluid catalytic cracking zone 700, and minor proportions ofdistillates and hydrotreated naphtha 308. The hydrotreated gas oilfraction 304 generally contains the portion of the vacuum gas oilhydrotreater 300 effluent that is at or above the AGO, H-AGO or VGOrange.

For instance, a suitable gas oil hydrotreating zone 300 can include, butis not limited to, systems based on technology commercially availablefrom Honeywell UOP, US; Chevron Lummus Global LLC (CLG), US; Axens, IFPGroup Technologies, FR; or Shell Global Solutions, US.

The gas oil hydrotreating zone 300 can contain one or more fixed-bed,ebullated-bed, slurry-bed, moving bed, continuous stirred tank (CSTR) ortubular reactors, in series and/or parallel arrangement. Additionalequipment, including exchangers, furnaces, feed pumps, quench pumps, andcompressors to feed the reactor(s) and maintain proper operatingconditions, are well known and are considered part of the gas oilhydrotreating zone 300. In addition, equipment, including pumps,compressors, high temperature separation vessels, low temperatureseparation vessels and the like to separate reaction products andprovide hydrogen recycle within the gas oil hydrotreating zone 300, arewell known and are considered part of the gas oil hydrotreating zone300.

An effective quantity of catalyst is provided in gas oil hydrotreatingzone 300, including those possessing hydrotreating functionality, forhydrodesulfurization and hydrodenitrification. Such catalyst generallycontain one or more active metal component of metals or metal compounds(oxides or sulfides) selected from the Periodic Table of the ElementsIUPAC Groups 6-10. In certain embodiments, the active metal component isone or more of Co, Ni, W and Mo. The active metal component is typicallydeposited or otherwise incorporated on a support, such as amorphousalumina, amorphous silica alumina, zeolites, or combinations thereof. Incertain embodiments, the catalyst used in the gas oil hydrotreating zone300 includes one or more beds selected from Co/Mo, Ni/Mo, Ni/W, andCo/Ni/Mo. Combinations of one or more beds of Co/Mo, Ni/Mo, Ni/W andCo/Ni/Mo, can also be used. The combinations can be composed ofdifferent particles containing a single active metal species, orparticles containing multiple active species. In certain embodiments, acombination of Co/Mo catalyst and Ni/Mo catalyst are effective forhydrodesulfurization and hydrodenitrification. One or more series ofreactors can be provided, with different catalysts in the differentreactors of each series. For instance, a first reactor includes Co/Mocatalyst and a second reactor includes Ni/Mo catalyst. Suitable catalystused in the gas oil hydrotreating zone 300 have an expected lifetime inthe range of about 28-44, 28-38, 34-44 or 34-38 months.

In certain embodiments, the gas oil hydrotreating zone 300 operatingconditions include:

a reactor inlet temperature (° C.) in the range of from about 324-496,324-453, 324-431, 367-496, 367-453, 367-431, 389-496, 389-453, 389-431or 406-414;

a reactor outlet temperature (° C.) in the range of from about 338-516,338-471, 338-449, 382-516, 382-471, 382-449, 404-516, 404-471, 404-449or 422-430;

a start of run (SOR) reaction temperature (° C.), as a weighted averagebed temperature (WABT), in the range of from about 302-462, 302-422,302-402, 342-462, 342-422, 342-402, 362-462, 362-422, 362-402 or378-384;

an end of run (EOR) reaction temperature (° C.), as a WABT, in the rangeof from about 333-509, 333-465, 333-443, 377-509, 377-465, 377-443,399-509, 399-465, 399-443 or 416-424;

a reaction inlet pressure (barg) in the range of from about 91-137,91-125, 91-119, 102-137, 102-125, 102-119, 108-137, 108-125, 108-119 or110-116;

a reaction outlet pressure (barg) in the range of from about 85-127,85-117, 85-111, 96-127, 96-117, 96-111, 100-127, 100-117 or 100-111;

a hydrogen partial pressure (barg) (outlet) in the range of from about63-95, 63-87, 63-83, 71-95, 71-87, 71-83, 75-95, 75-87, 75-83 or 77-81;

a hydrogen treat gas feed rate (SLt/Lt) up to about 525, 510, 465 or445, in certain embodiments from about 335-510, 335-465, 335-445,380-510, 380-465, 380-445, 400-510, 400-465 or 400-445;

a hydrogen quench gas feed rate (SLt/Lt) up to about 450, 430, 392 or375, in certain embodiments from about 285-430, 285-392, 285-375,320-430, 320-392, 320-375, 338-430, 338-392 or 338-375;

a make-up hydrogen feed rate (SLt/Lt) up to about 220, 200, 180 or 172,in certain embodiments from about 130-200, 130-180, 130-172, 148-200,148-180, 148-172, 155-200, 155-180 or 155-172; and

liquid hourly space velocity values (h⁻¹), on a fresh feed basisrelative to the hydrotreating catalysts, in the range of from about0.1-10.0, 0.1-5.0, 0.1-2.0, 0.3-10.0, 0.3-5.0, 0.3-2.0, 0.4-10.0,0.4-5.0, 0.4-3.0 or 0.5-2.5.

An effective quantity of catalyst is provided in gas oil hydrotreatingzone 300, including those possessing hydrotreating functionality, forhydrodesulfurization and hydrodenitrification. Such catalyst generallycontain one or more active metal component of metals or metal compounds(oxides or sulfides) selected from the Periodic Table of the ElementsIUPAC Groups 6-10. In certain embodiments, the active metal component isone or more of Co, Ni, W and Mo. The active metal component is typicallydeposited or otherwise incorporated on a support, such as amorphousalumina, amorphous silica alumina, zeolites, or combinations thereof. Incertain embodiments, the catalyst used in the gas oil hydrotreating zone300 includes one or more beds selected from Co/Mo, Ni/Mo, Ni/W, andCo/Ni/Mo. Combinations of one or more beds of Co/Mo, Ni/Mo, Ni/W andCo/Ni/Mo, can also be used. The combinations can be composed ofdifferent particles containing a single active metal species, orparticles containing multiple active species. In certain embodiments, acombination of Co/Mo catalyst and Ni/Mo catalyst are effective forhydrodesulfurization and hydrodenitrification. One or more series ofreactors can be provided, with different catalysts in the differentreactors of each series. For instance, a first reactor includes Co/Mocatalyst and a second reactor includes Ni/Mo catalyst. Effective liquidhourly space velocity values (h⁻¹), on a fresh feed basis relative tothe hydrotreating catalysts, are in the range of from about 0.1-10.0,0.1-5.0, 0.1-2.0, 0.3-10.0, 0.3-5.0, 0.3-2.0, 0.4-10.0, 0.4-5.0, 0.4-3.0or 0.5-2.5. Suitable catalyst used in the gas oil hydrotreating zone 300have an expected lifetime in the range of about 28-44, 28-38, 34-44 or34-38 months.

Under the above conditions and catalyst selections, exemplary productsfrom the gas oil hydrotreating zone 300 include 1-30, 5-30, 2-27 or 5-27wt % of effluent (relative to the feed to the gas oil hydrotreating zone300) boiling at or below the atmospheric residue end boiling point, suchas 370° C., including LPG, kerosene, naphtha, and atmospheric gas oilrange components. The remaining bottoms fraction is the hydrotreated gasoil fraction, all or a portion of which can be effectively integrated asfeed to the gas oil steam cracking zone 250 as described herein.

In additional embodiments, the gas oil hydrotreating zone 300 canoperate under conditions effective for feed conditioning and to maximizetargeted conversion to petrochemicals in the steam cracker complex.Accordingly, in certain embodiments severity conditions are selectedthat achieve objectives differing from those used for conventionalrefinery operations. That is, while typical VGO hydrotreating operateswith less emphasis on conservation of liquid product yield, in thepresent embodiment VGO hydrotreating operates to produce a higher yieldof lighter products which are intentionally recovered to maximizechemicals yield. In embodiments to maximize conversion topetrochemicals, the gas oil hydrotreating zone 300 operating conditionsinclude:

a reactor inlet temperature (° C.) in the range of from about 461-496,461-473, 485-496 or 473-485;

a reactor outlet temperature (° C.) in the range of from about 480-516,480-489, 489-495 or 495-516;

a start of run (SOR) reaction temperature (° C.), as a weighted averagebed temperature (WABT), in the range of from about 430-462, 430-440,440-450 or 450-462;

an end of run (EOR) reaction temperature (° C.), as a WABT, in the rangeof from about 473-509, 484-495, 473-484 or 495-509;

a reaction inlet pressure (barg) in the range of from about 110-137,113-137, 110-120, 120-129 or 129-137;

a reaction outlet pressure (barg) in the range of from about 104-118,104-108, 112-118 or 108-112;

a hydrogen partial pressure (barg) (outlet) in the range of from about76-95, 76-83, 83-89, or 89-95;

a hydrogen treat gas feed rate (SLt/Lt) up to about 525, 485, 490 or520, in certain embodiments from about 474-520, 474-488, 488-500, or500-520;

a hydrogen quench gas feed rate (SLt/Lt) up to about 450, 441, 416 or429, in certain embodiments from about 400-441, 400-415, 415-430, or430-441;

a make-up hydrogen feed rate (SLt/Lt) up to about 220, 200, 207 or 214,in certain embodiments from about 186-200, 190-200, 186-190, 190-195, or195-200; and

liquid hourly space velocity values (h⁻¹), on a fresh feed basisrelative to the hydrotreating catalysts, in the range of from about0.5-0.7, 0.5-0.55, 0.55-0.6, 0.6-0.65, 0.65-0.7.

Under the above conditions and catalyst selections, exemplary productsfrom the gas oil hydrotreating zone 300 operating under conditionseffective for feed conditioning and to maximize targeted conversion topetrochemicals in the steam cracker complex include 20-30, 22-28, 23-27or 24-26 wt % of effluent (relative to the feed to the gas oilhydrotreating zone 300) boiling at or below the atmospheric residue endboiling point, such as 370° C., including LPG, kerosene, naphtha, andatmospheric gas oil range components. The remaining bottoms fraction isthe hydrotreated gas oil fraction, all or a portion of which can beeffectively integrated as feed to the gas oil steam cracking zone 250 asdescribed herein.

In certain embodiments, the gas oil hydrotreating zone 300 contains oneor more trains of reactors, with a first reactor having two catalystbeds with two quench streams including an inter-bed quench stream, and asecond reactor (lag reactor) having one catalyst bed with a quenchstream. In high capacity operations, two or more parallel trains ofreactors are utilized. In such embodiments, the flow in gas oilhydrotreating zone 300 is split after the feed pump into paralleltrains, wherein each train contains feed/effluent heat exchangers, feedheater, a reactor and the hot separator. The trains recombine after thehot separators. Tops from the hot separators are combined and passed toa cold separator. Bottoms from the hot separators are passed to a hotflash drum. Bottoms from the cold separator and tops from the hot flashdrum are passed to a low pressure flash drum to remove off-gases. Hotflash liquid bottoms and low pressure flash bottoms are passed to astripper to recover hydrotreated gas oil and wild naphtha. Tops from thecold separator are subjected to absorption and amine scrubbing. Recyclehydrogen is recovered, and passed (along with make-up hydrogen) to thereaction zone as treat gas and quench gas.

FIG. 13 depicts a hydrocracking mode of operation for treatment of thevacuum gas oil. Hydrocracking processes are used commercially in a largenumber of petroleum refineries. They are used to process a variety offeeds boiling above the atmospheric gas oil range (for example, in therange of about 370 to 520° C.) in conventional hydrocracking units andboiling above the vacuum gas oil range (for example, above about 520°C.) in residue hydrocracking units. In general, hydrocracking processessplit the molecules of the feed into smaller, i.e., lighter, moleculeshaving higher average volatility and economic value. Additionally,hydrocracking processes typically improve the quality of the hydrocarbonfeedstock by increasing the hydrogen-to-carbon ratio and by removingorganosulfur and organonitrogen compounds. The significant economicbenefit derived from hydrocracking processes has resulted in substantialdevelopment of process improvements and more active catalysts.

Three major hydrocracking process schemes include single-stage oncethrough hydrocracking, series-flow hydrocracking with or withoutrecycle, and two-stage recycle hydrocracking. Single-stage once throughhydrocracking is the simplest of the hydrocracker configuration andtypically occurs at operating conditions that are more severe thanhydrotreating processes, and less severe than conventional higherpressure hydrocracking processes. It uses one or more reactors for bothtreating steps and cracking reaction, so the catalyst must be capable ofboth hydrotreating and hydrocracking. This configuration is costeffective, but typically results in relatively low product yields (forexample, a maximum conversion rate of about 50 wt %). Single stagehydrocracking is often designed to maximize mid-distillate yield over asingle or dual catalyst systems. Dual catalyst systems can be used in astacked-bed configuration or in two different reactors. The effluentsare passed to a fractionator column to separate the H₂S, NH₃, lightgases (C₁-C₄), naphtha and diesel products, boiling in the temperaturerange including and below atmospheric gas oil range fractions (forinstance in the temperature range of 36-370° C.). The hydrocarbonsboiling above the atmospheric gas oil range (for instance 370° C.) aretypically unconverted oils. Any portion of these unconverted oils thatare not recycled are drawn from a bottoms fraction in a gas oilhydrocracking zone 320 as a hydrogen-rich bleed stream and iseffectively integrated as feed to the high olefinic fluid catalyticcracking zone 700 as described herein. In certain embodiments,unconverted oils can be processed in a lube oil production unit (notshown).

The gas oil hydrocracking zone 320 operates under mild, moderate orsevere hydrocracking conditions, and generally produces off-gas andlight ends (not shown), a wild naphtha stream 326, a diesel fuelfraction 322, and an unconverted oil fraction 324. Effluent off-gasesare recovered from the gas oil hydrotreating zone 300 and are passed tothe olefins recovery train, the saturated gas plant as part of the othergases stream 156, and/or directly to a fuel gas system. Liquefiedpetroleum gas can be recovered from the gas oil hydrocracking zone 320and routed to the mixed feed steam cracking zone, the olefins recoverytrain and/or the saturated gas plant. The naphtha fraction 326 is routedto the mixed feed steam cracking zone 230. In certain embodiments, thenaphtha fraction 326 is routed through the crude complex 100, alone, orin combination with other wild naphtha fractions from within theintegrated process. In embodiments in which naphtha fraction 326 isrouted through the crude complex 100, all or a portion of the liquefiedpetroleum gas produced in the gas oil hydrocracking zone 320 can bepassed with the naphtha fraction 326. The unconverted oil fraction 324is routed to the high olefinic fluid catalytic cracking zone 700. Thediesel fuel fraction 322 is recovered as fuel, for instance, compliantwith Euro V diesel standards, and can be combined with the diesel fuelfraction 182 from the diesel hydrotreating zone 180. Vacuum gas oilhydrocracker 320 can operate under mild, moderate or severe conditions,depending on factors including the feedstock and the desired degree ofconversion

The gasoil hydrocracking zone 320 can operate under mild, moderate orsevere conditions, depending on factors including the feedstock and thedesired degree of conversion. Such conditions are effective for removalof a significant amount of the sulfur and other known contaminants, andfor conversion of the feed(s) into a major proportion of hydrocrackedproducts and minor proportions of off-gases, light ends and unconvertedproduct that is passed to the high olefinic fluid catalytic crackingzone 700.

For instance, a suitable vacuum gas oil hydrocracker zone 320 caninclude, but is not limited to, systems based on technology commerciallyavailable from Honeywell UOP, US; Chevron Lummus Global LLC (CLG), US;Axens, IFP Group Technologies, FR; or Shell Global Solutions, US.

The gas oil hydrocracking zone 320 can contain one or more fixed-bed,ebullated-bed, slurry-bed, moving bed, continuous stirred tank (CSTR) ortubular reactors, in series and/or parallel arrangement. Additionalequipment, including exchangers, furnaces, feed pumps, quench pumps, andcompressors to feed the reactor(s) and maintain proper operatingconditions, are well known and are considered part of the gas oilhydrocracking zone 320. In addition, equipment, including pumps,compressors, high temperature separation vessels, low temperatureseparation vessels and the like to separate reaction products andprovide hydrogen recycle within the gas oil hydrocracking zone 320, arewell known and are considered part of the gas oil hydrocracking zone320.

Series-flow hydrocracking with or without recycle is one of the mostcommonly used configuration. It uses one reactor (containing bothtreating and cracking catalysts) or two or more reactors for bothtreating and cracking reaction steps. In a series-flow configuration theentire hydrocracked product stream from the first reaction zone,including light gases (typically C₁-C₄, H₂S, NH₃) and all remaininghydrocarbons, are sent to the second reaction zone. Unconverted bottomsfrom the fractionator column are recycled back into the first reactorfor further cracking. This configuration converts heavy crude oilfractions such as vacuum gas oil, into light products and has thepotential to maximize the yield of naphtha, kerosene and or diesel rangehydrocarbons, depending on the recycle cut point used in thedistillation section.

Two-stage recycle hydrocracking uses two reactors and unconvertedbottoms from the fractionation column are passed to the second reactorfor further cracking. Since the first reactor accomplishes bothhydrotreating and hydrocracking, the feed to second reactor is virtuallyfree of ammonia and hydrogen sulfide. This permits the use of highperformance zeolite catalysts which are susceptible to poisoning bysulfur or nitrogen compounds.

Effective hydrocracking catalyst generally contain about 5-40 wt % basedon the weight of the catalyst, of one or more active metal component ofmetals or metal compounds (oxides or sulfides) selected from thePeriodic Table of the Elements IUPAC Groups 6-10. In certainembodiments, the active metal component is one or more of Mo, W, Co orNi. The active metal component is typically deposited or otherwiseincorporated on a support, such as amorphous alumina, amorphous silicaalumina, zeolites, or combinations thereof. In certain embodiments,alone or in combination with the above metals, Pt group metals such asPt and/or Pd, may be present as a hydrogenation component, generally inan amount of about 0.1-2 wt % based on the weight of the catalyst.Suitable hydrocracking catalyst have an expected lifetime in the rangeof about 18-30, 22-30, 18-26 or 22-26 months.

Exemplary products from the gas oil hydrocracking zone 320 include27-99, 27-90, 27-82, 27-80, 27-75, 27-52, 27-48, 30-99, 30-90, 30-82,30-80, 30-75, 30-52, 30-48, 48-99, 48-90, 48-82, 48-80, 48-75, 48-52,78-99, 78-90, 78-85, 80-90 or 80-99 wt % of effluent (relative to thefeed to the gas oil hydrocracking zone 320) boiling at or below theatmospheric residue end boiling point, such as 370° C., including LPG,kerosene, naphtha, and atmospheric gas oil range components. Theremaining bottoms fraction is the unconverted oil fraction, all or aportion of which can be effectively integrated as feed to the higholefinic fluid catalytic cracking zone 700 as described herein.

FIG. 18 schematically depicts an embodiment of a once-through singlereactor hydrocracking zone 330 including a reaction zone 332 and afractionating zone 342, which can as a mild conversion or partialconversion hydrocracker.

Reaction zone 332 generally includes one or more inlets in fluidcommunication with a source of initial feedstock 334 and a source ofhydrogen gas 338. One or more outlets of reaction zone 332 thatdischarge effluent stream 340 is in fluid communication with one or moreinlets of the fractionating zone 342 (typically including one or morehigh pressure and/or low pressure separation stages therebetween forrecovery of recycle hydrogen, not shown).

Fractionating zone 342 includes one or more outlets for discharginggases 344, typically H₂, H₂S, NH₃, and light hydrocarbons (C₁-C₄); oneor more outlets for recovering product 346, such as middle distillatesnaphtha and diesel products boiling in the temperature range includingand below atmospheric gas oil range fractions (for instance in thetemperature range of 36-370° C.); and one or more outlets fordischarging bottoms 348 including hydrocarbons boiling above theatmospheric gas oil range (for instance 370° C.). In certainembodiments, the temperature cut point for bottoms 348 (andcorrespondingly the end point for the products 346) is a rangecorresponding to the upper temperature limit of the desired gasoline,kerosene and/or diesel product boiling point ranges for downstreamoperations.

In operation of the once-through single reactor hydrocracking zone 330,a feedstock stream 334 and a hydrogen stream 338 are charged to thereaction zone 332. Hydrogen stream 338 is an effective quantity ofhydrogen to support the requisite degree of hydrocracking, feed type,and other factors, and can be any combination including, recyclehydrogen 336 from optional gas separation subsystems (not shown)associated with reaction zone 332, and/or derived from fractionator gasstream 344 and make-up hydrogen 302, if necessary. In certainembodiments, a reaction zone can contain multiple catalyst beds and canreceive one or more quench hydrogen streams between the beds (notshown).

The reaction effluent stream 340 contains converted, partially convertedand unconverted hydrocarbons. Reaction effluent stream 340 is passed tofractionating zone 342 (optionally after one or more high pressure andlow pressure separation stages to recover recycle hydrogen), generallyto recover gas and liquid products and by-products 344, 346, andseparate a bottoms fraction 348. This stream 348 is routed to the higholefinic fluid catalytic cracking zone 700 as described herein.

Gas stream 344, typically containing H₂, H₂S, NH₃, and lighthydrocarbons (C₁-C₄), is discharged and recovered and can be furtherprocessed. Effluent off-gases are passed to the olefins recovery train,the saturated gas plant as part of the other gases stream 156, and/ordirectly to a fuel gas system. Liquefied petroleum gas can be recoveredand routed to the mixed feed steam cracking zone, the olefins recoverytrain and/or the saturated gas plant. One or more cracked productstreams 346 are discharged via appropriate outlets of the fractionatorand can be further processed and/or blended in downstream refineryoperations to produce gasoline, kerosene and/or diesel fuel, or otherpetrochemical products.

In certain embodiments (not shown), fractionating zone 342 can operateas a flash vessel to separate heavy components at a suitable cut point,for example, a range corresponding to the upper temperature range of thedesired gasoline, kerosene and/or diesel products for downstreamoperations. In certain embodiments, a suitable cut point is in the rangeof 350 to 450° C., 360 to 450° C., 370 to 450° C., 350 to 400° C., 360to 400° C., 370 to 400° C., 350 to 380° C., or 360 to 380° C. The streamabove that cut point is routed to the high olefinic fluid catalyticcracking zone 700 as described herein.

For instance, a suitable once-through single reactor hydrocracking zone330 can include, but is not limited to, systems based on technologycommercially available from Honeywell UOP, US; Chevron Lummus Global LLC(CLG), US; Axens, IFP Group Technologies, FR; or Shell Global Solutions,US.

The reactor arrangement in the once-through single reactor hydrocrackingzone 330 can contain one or more fixed-bed, ebullated-bed, slurry-bed,moving bed, continuous stirred tank (CSTR), or tubular reactors, whichcan be in parallel arrangement. The once-through single reactorhydrocracking zone 330 can operate in a mild hydrocracking mode ofoperation or a partial conversion mode of operation. Additionalequipment, including exchangers, furnaces, feed pumps, quench pumps, andcompressors to feed the reactor(s) and maintain proper operatingconditions, are well known and are considered part of the once-throughsingle reactor hydrocracking zone 330. In addition, equipment, includingpumps, compressors, high temperature separation vessels, low temperatureseparation vessels and the like to separate reaction products andprovide hydrogen recycle within the once-through single reactorhydrocracking zone 330, are well known and are considered part of theonce-through single reactor hydrocracking zone 330.

In certain embodiments, operating conditions for the reactor(s) inhydrocracking zone 330 using a once-through (single stage withoutrecycle) configuration and operating in a mild hydrocracking modeinclude:

a reactor inlet temperature (° C.) in the range of from about 329-502,329-460, 329-440, 372-502, 372-460, 372-440, 394-502, 394-460, 394-440or 412-420;

a reactor outlet temperature (° C.) in the range of from about 338-516,338-471, 338-450, 382-516, 382-471, 382-450, 400-516, 400-471, 400-450or 422-430;

a start of run (SOR) reaction temperature, as a weighted average bedtemperature (WABT), in the range of from about 310-475, 310-435,310-415, 350-475, 350-435, 350-415, 370-475, 370-435, 370-415 or390-397;

an end of run (EOR) reaction temperature, as a WABT, in the range offrom about 338-516, 338-471, 338-450, 382-516, 382-471, 382-450,400-516, 400-471, 400-450 or 422-430;

a reaction inlet pressure (barg) in the range of from about 108-161,108-148, 108-141, 121-161, 121-148, 121-141, 128-161, 128-148, 128-141or 131-137;

a reaction outlet pressure (barg) in the range of from about 100-150,100-137, 100-130, 112-150, 112-137, 112-130, 118-150, 118-137 or118-130;

a hydrogen partial pressure (barg) (outlet) in the range of from about77-116, 77-106, 77-101, 87-116, 87-106, 87-101, 92-116, 92-106, 92-101or 94-98;

a hydrogen treat gas feed rate (SLt/Lt) up to about 530, 510, 470 or450, in certain embodiments from about 340-510, 340-470, 340-450,382-510, 382-470, 382-450, 400-510, 400-470, 400-450 or 410-440;

a hydrogen quench gas feed rate (SLt/Lt) up to about 470, 427, 391 or356, in certain embodiments from about 178-427, 178-214, 178-356,214-321 or 178-391;

make-up hydrogen rate (SLt/Lt) up to about 225, 215, 200 or 190, incertain embodiments from about 143-215, 143-200, 143-190, 161-215,161-200, 161-190, 170-215, 170-200 or 170-190; and

liquid hourly space velocity values (h⁻¹), on a fresh feed basisrelative to the hydrocracking catalysts, are in the range of from about0.1-10.0, 0.1-5.0, 0.1-2.0, 0.3-10.0, 0.3-5.0, 0.3-2.0, 0.4-10.0,0.4-5.0 or 0.5-3.0.

Under the above conditions and catalyst selections, exemplary productsfrom the once-through single reactor hydrocracking zone 330 operating ina mild hydrocracking mode of operation include 27-52, 27-48, 30-50 or30-52 wt % of effluent (relative to the feed to the gas oilhydrotreating zone 330) boiling at or below the atmospheric residue endboiling point, such as 370° C., including LPG, kerosene, naphtha, andatmospheric gas oil range components. The remaining bottoms fraction isthe unconverted oil fraction, all or a portion of which can beeffectively integrated as feed to the high olefinic fluid catalyticcracking zone 700 as described herein.

In certain embodiments, operating conditions for the reactor(s) inhydrocracking zone 330 using a once-through (single stage withoutrecycle) configuration and operating in a partial conversion modeinclude:

a reactor inlet temperature (° C.) in the range of from about 340-502,340-460, 340-440, 372-502, 372-460, 372-440, 394-502, 394-460, 394-440or 412-420;

a reactor outlet temperature (° C.) in the range of from about 350-516,350-471, 350-450, 382-516, 382-471, 382-450, 400-516, 400-471, 400-450or 422-430;

a start of run (SOR) reaction temperature, as a weighted average bedtemperature (WABT), in the range of from about 310-475, 310-435,310-415, 350-475, 350-435, 350-415, 370-475, 370-435, 370-415 or390-397;

an end of run (EOR) reaction temperature, as a WABT, in the range offrom about 338-516, 338-471, 338-450, 382-516, 382-471, 382-450,400-516, 400-471, 400-450 or 422-430;

a reaction inlet pressure (barg) in the range of from about 100-165,100-150, 100-140, 120-165, 120-140, 130-165, 130-150, or 130-140;

a reaction outlet pressure (barg) in the range of from about 92-150,92-137, 92-130, 112-150, 112-127, 112-130, 118-140, 118-130;

a hydrogen partial pressure (barg) (outlet) in the range of from about80-120, 80-106, 80-101, 90-120, 90-106, 90-101, 100-120, or 100-115;

a hydrogen treat gas feed rate (SLt/Lt) up to about 677, 615, 587 or573, in certain embodiments from about 503-615, 503-587, 503-573,531-615, 531-587, 531-573, 545-615, 545-587, or 545-573;

a hydrogen quench gas feed rate (SLt/Lt) up to about 614, 558, 553 or520, in certain embodiments from about 457-558, 457-533, 457-520,482-558, 482-533, 482-520, 495-558, 495-533, or 495-520;

make-up hydrogen rate (SLt/Lt) up to about 305, 277, 264 or 252, incertain embodiments from about 204-277, 204-264, 204-252, 216-277,216-264, 216-252, 228-277, 228-264, or 228-252; and

liquid hourly space velocity values (h⁻¹), on a fresh feed basisrelative to the hydrocracking catalysts, are in the range of from about0.1-10.0, 0.1-5.0, 0.1-2.0, 0.3-10.0, 0.3-5.0, 0.3-2.0, 0.4-10.0,0.4-5.0, 0.4-2.0 or 0.5-3.0.

Under the above conditions and catalyst selections, exemplary productsfrom the once-through single reactor hydrocracking zone 330 operating asa partial conversion hydrocracker include 48-82, 50-80, 48-75, 50-75 wt% of effluent (relative to the feed to the gas oil hydrotreating zone330) boiling at or below the atmospheric residue end boiling point, suchas 370° C., including LPG, kerosene, naphtha, and atmospheric gas oilrange components. The remaining bottoms fraction is the unconverted oilfraction, all or a portion of which can be effectively integrated asfeed to the high olefinic fluid catalytic cracking zone 700 as describedherein.

FIG. 19 schematically depicts another embodiment of a series flowhydrocracking zone 350, which operates as series-flow hydrocrackingsystem with recycle to the first reactor zone, the second reactor zone,or both the first and second reactor zones. In general, series flowhydrocracking zone 350 includes a first reaction zone 352, a secondreaction zone 358 and a fractionating zone 342.

First reaction zone 352 generally includes one or more inlets in fluidcommunication with a source of initial feedstock 334, a source ofhydrogen gas 338, and in certain embodiments recycle stream 364 acomprising all or a portion of the fractionating zone 342 bottoms stream348 and optionally a portion of fractionating zone 342 product stream362. One or more outlets of the first reaction zone 352 that dischargeeffluent stream 354 is in fluid communication with one or more inlets ofthe second reaction zone 358. In certain embodiments, the effluents 354are passed to the second reaction zone 358 without separation of anyexcess hydrogen and light gases. In optional embodiments, one or morehigh pressure and low pressure separation stages are provided betweenthe first and second reaction zones 352, 358 for recovery of recyclehydrogen (not shown).

The second reaction zone 358 generally includes one or more inlets influid communication with one or more outlets of the first reaction zone352, optionally a source of additional hydrogen gas 356, and in certainembodiments a recycle stream 364 b comprising all or a portion of thefractionating zone 342 bottoms stream 348 and optionally a portion offractionating zone 342 product stream 362. One or more outlets of thesecond reaction zone 358 that discharge effluent stream 360 is in fluidcommunication with one or more inlets of the fractionating zone 342(optionally having one or more high pressure and low pressure separationstages therebetween for recovery of recycle hydrogen, not shown).

Fractionating zone 342 includes one or more outlets for discharginggases 344, typically H₂, H₂S, NH₃, and light hydrocarbons (C₁-C₄); oneor more outlets for recovering product 346, such as middle distillatesnaphtha and diesel products boiling in the temperature range includingand below atmospheric gas oil range fractions (for instance in thetemperature range of 36-370° C.); and one or more outlets fordischarging bottoms 348 including hydrocarbons boiling above theatmospheric gas oil range (for instance about 370° C.), from which ableed stream 368 is obtained in processes that do not operate with 100%recycle. In certain embodiments, the temperature cut point for bottoms348 (and correspondingly the end point for the products 346) is a rangecorresponding to the upper temperature limit of the desired gasoline,kerosene and/or diesel product boiling point ranges for downstreamoperations.

In operation of the series flow hydrocracking zone 350, a feedstockstream 334 and a hydrogen stream 338 are charged to the first reactionzone 352. Hydrogen stream 338 is an effective quantity of hydrogen tosupport the requisite degree of hydrocracking, feed type, and otherfactors, and can be any combination including, recycle hydrogen 336 fromoptional gas separation subsystems (not shown) associated with reactionzones 352 and 358, and/or derived from fractionator gas stream 344 andmake-up hydrogen 302. In certain embodiments, a reaction zone cancontain multiple catalyst beds and can receive one or more quenchhydrogen streams between the beds (not shown).

First reaction zone 352 operates under effective conditions forproduction of reaction effluent stream 354 which is passed to the secondreaction zone 358 (optionally after one or more high pressure and lowpressure separation stages to recover recycle hydrogen), optionallyalong with an additional hydrogen stream 356. Second reaction zone 358operates under conditions effective for production of the reactioneffluent stream 360, which contains converted, partially converted andunconverted hydrocarbons.

The reaction effluent stream 360 is passed to fractionating zone 342,generally to recover gas and liquid products and by-products 344, 346,and separate a bottoms fraction 348. A portion of the bottoms fraction348, stream 368 is routed to the high olefinic fluid catalytic crackingzone 700 as described herein.

Gas stream 344, typically containing H₂, H₂S, NH₃, and lighthydrocarbons (C₁-C₄), is discharged and recovered and can be furtherprocessed. Effluent off-gases are passed to the olefins recovery train,the saturated gas plant as part of the other gases stream 156, and/ordirectly to a fuel gas system. Liquefied petroleum gas can be recoveredand routed to the mixed feed steam cracking zone, the olefins recoverytrain and/or the saturated gas plant. One or more cracked productstreams 346 are discharged via appropriate outlets of the fractionatorand can be further processed and/or blended in downstream refineryoperations to produce gasoline, kerosene and/or diesel fuel, or otherpetrochemical products. In certain embodiments, a diesel fraction 362derived from the one or more cracked product streams 346 can beintegrated with the recycle streams to the reactors. This integrationadds to the flexibility of the configuration between production ofdiesel fuel or petrochemicals from the product streams 346.

In certain embodiments (not shown), fractionating zone 342 can operateas a flash vessel to separate heavy components at a suitable cut point,for example, a range corresponding to the upper temperature range of thedesired gasoline, kerosene and/or diesel products for downstreamoperations. In certain embodiments, a suitable cut point is in the rangeof 350 to 450° C., 360 to 450° C., 370 to 450° C., 350 to 400° C., 360to 400° C., 370 to 400° C., 350 to 380° C., or 360 to 380° C. The streamabove that cut point is routed to the high olefinic fluid catalyticcracking zone 700 as described herein.

All or a portion of the fractionator bottoms stream 348 from thereaction effluent is recycled to the first or second reaction zones 352and/or 358 (streams 364 a and/or 364 b). In certain embodiments, aportion of the fractionator bottoms from the reaction effluent isremoved as bleed stream 368. Bleed stream 368 can be about 0-10 vol %,1-10 vol %, 1-5 vol % or 1-3 vol % of the fractionator bottoms 348. Thisstream 368 is routed to the high olefinic fluid catalytic cracking zone700 as described herein.

Accordingly, all or a portion of the fractionator bottoms stream 348 isrecycled to the second reaction zone 358 as stream 364 b, the firstreaction zone 352 as stream 364 a, or both the first and second reactionzones 352 and 358. For instance, stream 364 a recycled to zone 352comprises 0 to 100 vol %, in certain embodiments 0 to about 80 vol %,and in further embodiments 0 to about 50 vol % of stream 348, and stream364 b recycled to zone 358 comprises 0 to 100 vol %, in certainembodiments 0 to about 80 vol %, and in further embodiments 0 to about50 vol % of stream 348. In certain embodiments, in which the recycle isat or approaches 100 vol %, recycle of the unconverted oil increases theyield of products suitable as feed to the mixed feed steam cracking zone230.

For instance, a suitable series flow hydrocracking zone 350 can include,but is not limited to, systems based on technology commerciallyavailable from Honeywell UOP, US; Chevron Lummus Global LLC (CLG), US;Axens, IFP Group Technologies, FR; or Shell Global Solutions, US.

The reactor arrangement in the series flow hydrocracking zone 350 cancontain one or more fixed-bed, ebullated-bed, slurry-bed, moving bed,continuous stirred tank (CSTR), or tubular reactors, which can be inparallel arrangement. Additional equipment, including exchangers,furnaces, feed pumps, quench pumps, and compressors to feed thereactor(s) and maintain proper operating conditions, are well known andare considered part of the series flow hydrocracking zone 350. Inaddition, equipment, including pumps, compressors, high temperatureseparation vessels, low temperature separation vessels and the like toseparate reaction products and provide hydrogen recycle within theseries flow hydrocracking zone 350, are well known and are consideredpart of the series flow hydrocracking zone 350.

In certain embodiments, operating conditions for the first reactor(s) inhydrocracking zone 350 using once-through series configuration operatingin a partial conversion mode of operation include:

a reactor inlet temperature (° C.) in the range of from about 340-502,340-460, 340-440, 372-502, 372-460, 372-440, 394-502, 394-460, 394-440or 412-420;

a reactor outlet temperature (° C.) in the range of from about 350-516,350-471, 350-450, 382-516, 382-471, 382-450, 400-516, 400-471, 400-450or 422-430;

a start of run (SOR) reaction temperature, as a weighted average bedtemperature (WABT), in the range of from about 310-475, 310-435,310-415, 350-475, 350-435, 350-415, 370-475, 370-435, 370-415 or390-397;

an end of run (EOR) reaction temperature, as a WABT, in the range offrom about 338-516, 338-471, 338-450, 382-516, 382-471, 382-450,400-516, 400-471, 400-450 or 422-430;

a reaction inlet pressure (barg) in the range of from about 100-165,100-150, 100-140, 120-165, 120-140, 130-165, 130-150, or 130-140;

a reaction outlet pressure (barg) in the range of from about 92-150,92-137, 92-130, 112-150, 112-127, 112-130, 118-140, 118-130;

a hydrogen partial pressure (barg) (outlet) in the range of from about80-120, 80-106, 80-101, 90-120, 90-106, 90-101, 100-120, or 100-115;

a hydrogen treat gas feed rate (SLt/Lt) up to about 668, 607, 580 or566, in certain embodiments from about 497-607, 497-580, 497-566,525-607, 525-580, 525-566, 538-607, 538-580, or 538-566;

a hydrogen quench gas feed rate (SLt/Lt) up to about 819, 744, 711 or694, in certain embodiments from about 609-744, 609-711, 609-694,643-744, 643-711, 643-694, 660-744, 660-711, or 660-694;

make-up hydrogen rate (SLt/Lt) up to about 271, 246, 235 or 224, incertain embodiments from about 182-246, 182-235, 182-224, 192-246,192-235, 192-224, 203-246, 203-235, or 203-224; and

liquid hourly space velocity values (h⁻¹), on a fresh feed basisrelative to the hydrocracking catalysts, are in the range of from about0.1-10.0, 0.1-5.0, 0.1-2.0, 0.3-10.0, 0.3-5.0, 0.3-2.0, 0.4-10.0,0.4-5.0, 0.4-2.0 or 0.5-1.5.

In certain embodiments, operating conditions for the second reactor(s)in hydrocracking zone 350 using once-through series configurationoperating in a partial conversion mode of operation include:

In certain embodiments, partial conversion hydrocracking usingonce-through configuration operating conditions include:

a reactor inlet temperature (° C.) in the range of from about 340-502,340-460, 340-440, 372-502, 372-460, 372-440, 394-502, 394-460, 394-440or 412-420;

a reactor outlet temperature (° C.) in the range of from about 350-516,350-471, 350-450, 382-516, 382-471, 382-450, 400-516, 400-471, 400-450or 422-430;

a start of run (SOR) reaction temperature, as a weighted average bedtemperature (WABT), in the range of from about 310-475, 310-435,310-415, 350-475, 350-435, 350-415, 370-475, 370-435, 370-415 or390-397;

an end of run (EOR) reaction temperature, as a WABT, in the range offrom about 338-516, 338-471, 338-450, 382-516, 382-471, 382-450,400-516, 400-471, 400-450 or 422-430;

a reaction inlet pressure (barg) in the range of from about 90-150,90-130, 90-140, 110-150, 110-130, 110-145, or 130-150;

a reaction outlet pressure (barg) in the range of from about 85-140,85-127, 100-140, 112-130, 112-140, or 118-130;

hydrogen partial pressure (barg) (outlet) in the range of from about80-130, 80-120, 80-101, 90-130, 90-120, 90-101, 100-130, or 100-115;

a hydrogen treat gas feed rate (SLt/Lt) up to about 890, 803, 767 or748, in certain embodiments from about 657-803, 657-767, 657-748,694-803, 694-767, 694-748, 712-803, 712-767, or 712-748;

a hydrogen quench gas feed rate (SLt/Lt) up to about 850, 764, 729 or712, in certain embodiments from about 625-764, 625-729, 625-712,660-764, 660-729, 660-712, 677-764, 677-729, or 677-712;

make-up hydrogen rate (SLt/Lt) up to about 372, 338, 323 or 309, incertain embodiments from about 250-338, 250-323, 250-309, 264-338,264-323, 264-309, 279-338, 279-323, or 279-309; and

liquid hourly space velocity values (h⁻¹), on a fresh feed basisrelative to the hydrocracking catalysts, are in the range of from about0.1-10.0, 0.1-5.0, 0.1-2.0, 0.3-10.0, 0.3-5.0, 1.0-5.0, 2.0-4.0 or1.0-3.0.

Under the above conditions and catalyst selections, exemplary productsfrom the partial conversion hydrocracker using once-throughconfiguration include 48-82, 50-80, 48-75 or 50-75 wt % of effluentboiling at or below the atmospheric residue end boiling point, such as370° C., including LPG, kerosene, naphtha, and atmospheric gas oil rangecomponents. The remaining bottoms fraction is the unconverted oilfraction, all or a portion of which can be effectively integrated asfeed to the high olefinic fluid catalytic cracking zone 700 as describedherein.

FIG. 20 schematically depicts another embodiment of an integratedhydrocracking unit operation, a two-stage with recycle hydrocrackingzone 370, which operates as two-stage hydrocracking system with recycle.In general, hydrocracking zone 370 includes a first reaction zone 372, asecond reaction zone 382 and a fractionating zone 342.

First reaction zone 372 generally includes one or more inlets in fluidcommunication with a source of initial feedstock 334 and a source ofhydrogen gas 338. One or more outlets of the first reaction zone 372that discharge effluent stream 374 are in fluid communication with oneor more inlets of the fractionating zone 342 (optionally having one ormore high pressure and low pressure separation stages therebetween forrecovery of recycle hydrogen, not shown).

Fractionating zone 342 includes one or more outlets for discharginggases 344, typically H₂S, NH₃, and light hydrocarbons (C₁-C₄); one ormore outlets for recovering product 346, such as naphtha and dieselproducts boiling in the temperature range including and belowatmospheric gas oil range fractions (for instance in the temperaturerange of 36-370° C.); and one or more outlets for discharging bottoms348 including hydrocarbons boiling above the atmospheric gas oil range(for instance about 370° C.), from which a bleed stream 368 is obtainedin processes that do not operate with 100% recycle. In certainembodiments, the temperature cut point for bottoms 348 (andcorrespondingly the end point for the products 346) is a rangecorresponding to the upper temperature limit of the desired gasoline,kerosene and/or diesel product boiling point ranges for downstreamoperations.

The fractionating zone 342 bottoms outlet is in fluid communication withthe one or more inlets of the second reaction zone 382 for recyclestream 348 a derived from the bottoms stream 348. Recycle stream 348 acan be all or a portion of the bottoms stream 348. In certain optionalembodiments (as indicated by dashed lines in FIG. 20), a portion 348 bis in fluid communication with one or more inlets of the first reactionzone 372.

Second reaction zone 382 generally includes one or more inlets in fluidcommunication with the fractionating zone 342 bottoms outlet portion 348a of bottoms 348, and a source of hydrogen gas 384. One or more outletsof the second reaction zone 382 that discharge effluent stream 386 arein fluid communication with one or more inlets of the fractionating zone342 (optionally having one or more high pressure and low pressureseparation stages therebetween for recovery of recycle hydrogen, notshown).

In operation of the two-stage hydrocracking zone 370, a feedstock stream334 and a hydrogen stream 338 are charged to the first reaction zone372. Hydrogen stream 338 is an effective quantity of hydrogen to supportthe requisite degree of hydrocracking, feed type, and other factors, andcan be any combination including, recycle hydrogen 336 from optional gasseparation subsystems (not shown) associated with reaction zones 372 and382, and/or derived from fractionator gas stream 344 and make-uphydrogen 302. In certain embodiments, a reaction zone can containmultiple catalyst beds and can receive one or more quench hydrogenstreams between the beds (not shown).

First reaction zone 372 operates under effective conditions forproduction of reaction effluent stream 374 which is passed to thefractionating zone 342 (optionally after one or more high pressure andlow pressure separation stages to recover recycle hydrogen) generally torecover gas and liquid products and by-products, and separate a bottomsfraction.

Gas stream 344, typically containing H₂, H₂S, NH₃, and lighthydrocarbons (C₁-C₄), is discharged and recovered and can be furtherprocessed. Effluent off-gases are passed to the olefins recovery train,the saturated gas plant as part of the other gases stream 156, and/ordirectly to a fuel gas system. Liquefied petroleum gas can be recoveredand routed to the mixed feed steam cracking zone, the olefins recoverytrain and/or the saturated gas plant. One or more cracked productstreams 346 are discharged via appropriate outlets of the fractionatorand can be further processed and/or blended in downstream refineryoperations to produce gasoline, kerosene and/or diesel fuel, or otherpetrochemical products. In certain embodiments, a diesel fraction 376derived from the one or more cracked product streams 346 can beintegrated with the feed to the second stage reactor 382. Thisintegration adds to the flexibility of the configuration betweenproduction of diesel fuel or petrochemicals from the product streams346.

In certain embodiments (not shown), fractionating zone 342 can operateas a flash vessel to separate heavy components at a suitable cut point,for example, a range corresponding to the upper temperature range of thedesired gasoline, kerosene and/or diesel products for downstreamoperations. In certain embodiments, a suitable cut point is in the rangeof 350 to 450° C., 360 to 450° C., 370 to 450° C., 350 to 400° C., 360to 400° C., 370 to 400° C., 350 to 380° C., or 360 to 380° C. The streamabove that cut point is routed to the high olefinic fluid catalyticcracking zone 700 as described herein.

All or a portion of the fractionator bottoms stream 348 from thereaction effluent is passed to the second reaction zone 382 as stream348 a. In certain embodiments, all or a portion of the bottoms stream348 is recycled to the second reaction zone 382 as stream 348 a, thefirst reaction zone 372 as stream 348 b, or both the first and secondreaction zones 372 and 382. For instance, stream 348 b which is recycledto zone 372 comprises 0 to 100 vol %, 0 to about 80 vol %, or 0 to about50 vol % of stream 348, and stream 348 a which is recycled to zone 382comprises 0 to 100 vol %, 0 to about 80 vol %, or 0 to about 50 vol % ofstream 348. In certain embodiments, in which the recycle is at orapproaches 100 vol %, recycle of the unconverted oil increases the yieldof products suitable as feed to the mixed feed steam cracking zone 230.

In certain embodiments, a portion of the fractionator bottoms from thereaction effluent is removed as bleed stream 368. Bleed stream 368 canbe about 0-10 vol %, 1-10 vol %, 1-5 vol % or 1-3 vol % of thefractionator bottoms 348.

Second reaction zone 382 operates under conditions effective forproduction of the reaction effluent stream 386, which containsconverted, partially converted and unconverted hydrocarbons. The secondstage the reaction effluent stream 386 is passed to the fractionatingzone 342, optionally through one or more gas separators to recoveryrecycle hydrogen and remove certain light gases

For instance, a suitable two-stage hydrocracking zone 370 can include,but is not limited to, systems based on technology commerciallyavailable from Honeywell UOP, US; Chevron Lummus Global LLC (CLG), US;Axens, IFP Group Technologies, FR; or Shell Global Solutions, US.

The reactor arrangement in the two-stage with recycle hydrocracking zone370 can contain one or more fixed-bed, ebullated-bed, slurry-bed, movingbed, continuous stirred tank (CSTR), or tubular reactors, which can bein parallel arrangement. Additional equipment, including exchangers,furnaces, feed pumps, quench pumps, and compressors to feed thereactor(s) and maintain proper operating conditions, are well known andare considered part of the two-stage hydrocracking zone 370. Inaddition, equipment, including pumps, compressors, high temperatureseparation vessels, low temperature separation vessels and the like toseparate reaction products and provide hydrogen recycle within thetwo-stage hydrocracking zone 370, are well known and are considered partof the two-stage hydrocracking zone 370.

In certain embodiments, operating conditions for the first stagereactor(s) in hydrocracking zone 370 using a two-stage with recycleconfiguration operating in a full conversion mode of operation include:

a reactor inlet temperature (° C.) in the range of from about 340-502,340-460, 340-440, 372-502, 372-460, 372-440, 394-502, 394-460, 394-440or 412-420;

a reactor outlet temperature (° C.) in the range of from about 350-516,350-471, 350-450, 382-516, 382-471, 382-450, 400-516, 400-471, 400-450or 422-430;

a start of run (SOR) reaction temperature, as a weighted average bedtemperature (WABT), in the range of from about 310-475, 310-435,310-415, 350-475, 350-435, 350-415, 370-475, 370-435, 370-415 or390-397;

an end of run (EOR) reaction temperature, as a WABT, in the range offrom about 338-516, 338-471, 338-450, 382-516, 382-471, 382-450,400-516, 400-471, 400-450 or 422-430;

a reaction inlet pressure (barg) in the range of from about 100-180,100-160, 100-141, 121-180, 121-160, 121-141, 128-180, 128-160, 128-141or 131-180;

a reaction outlet pressure (barg) in the range of from about 90-170,90-137, 90-130, 112-170, 112-137, 112-130, 118-150, 118-137 or 118-170;

a hydrogen partial pressure (barg) (outlet) in the range of from about90-137, 90-106, 90-120, 100-137, 100-106, or 100-120;

a hydrogen treat gas feed rate (SLt/Lt) up to about 1050, 940, 898 or876, in certain embodiments from about 769-940, 769-898, 769-876,812-940, 812-898, 812-876, 834-940, 834-898, or 834-876;

a hydrogen quench gas feed rate (SLt/Lt) up to about 1100, 980, 935 or913, in certain embodiments from about 801-980, 801-935, 801-913,846-980, 846-935, 846-913, 868-980, 868-935, or 868-913;

make-up hydrogen rate (SLt/Lt) up to about 564, 512, 490 or 468, incertain embodiments from about 378-512, 378-490, 378-468, 401-512,401-490, 401-468, 423-512, 423-490, or 423-468; and

liquid hourly space velocity values (h⁻¹), on a fresh feed basisrelative to the hydrocracking catalysts, are in the range of from about0.1-10.0, 0.1-5.0, 0.1-2.0, 0.3-10.0, 0.3-5.0, 0.3-2.0, 0.4-10.0,0.4-5.0, 0.4-2.0 or 0.5-1.5.

In certain embodiments, operating conditions for the second stagereactor(s) in hydrocracking zone 370 using a two-stage with recycleconfiguration operating in a full conversion mode of operation include:

In certain embodiments, operating conditions for the reactor(s) in thefirst stage reaction zone of the two-stage hydrocracking zone 370include:

a reactor inlet temperature (° C.) in the range of from about 340-502,340-460, 340-440, 372-502, 372-460, 372-440, 394-502, 394-460, 394-440or 412-420;

a reactor outlet temperature (° C.) in the range of from about 350-516,350-471, 350-450, 382-516, 382-471, 382-450, 400-516, 400-471, 400-450or 422-430;

a start of run (SOR) reaction temperature, as a weighted average bedtemperature (WABT), in the range of from about 310-475, 310-435,310-415, 350-475, 350-435, 350-415, 370-475, 370-435, 370-415 or390-397;

an end of run (EOR) reaction temperature, as a WABT, in the range offrom about 338-516, 338-471, 338-450, 382-516, 382-471, 382-450,400-516, 400-471, 400-450 or 422-430;

a reaction inlet pressure (barg) in the range of from about 80-145,80-100, 80-131, 80-120, 120-145, 100-145, or 130-145;

a reaction outlet pressure (barg) in the range of from about 75-137,75-130, 90-130, 100-137, 100-122, or 112-137;

a hydrogen partial pressure (barg) (outlet) in the range of from about90-145, 90-106, 90-120, 100-145, 100-106, or 100-120;

a hydrogen treat gas feed rate (SLt/Lt) up to about 910, 823, 785 or767, in certain embodiments from about 673-823, 673-785, 673-767,711-823, 711-785, 711-767, 729-823, 729-785, or 729-767;

a hydrogen quench gas feed rate (SLt/Lt) up to about 980, 882, 842 or822, in certain embodiments from about 721-882, 721-842, 721-822,761-882, 761-842, 761-822, 781-882, 781-842, or 781-822;

make-up hydrogen rate (SLt/Lt) up to about 451, 410, 392 or 374, incertain embodiments from about 303-410, 303-392, 303-374, 321-410,321-392, 321-374, 338-410, 338-392, or 338-374; and

liquid hourly space velocity values (h⁻¹), on a fresh feed basisrelative to the hydrocracking catalysts, are in the range of from about0.1-10.0, 0.1-5.0, 0.1-2.0, 0.3-10.0, 0.3-5.0, 1.0-5.0, 2.0-4.0 or1.0-3.0.

Under the above conditions and catalyst selections, exemplary productsfrom the hydrocracking zone 370 operating as a two-stage hydrocracker(with recycle) in a full conversion mode include 78-99, 78-90, 78-85,80-90 or 80-99 wt % of effluent (relative to the feed to thehydrocracking zone 370) boiling at or below the atmospheric residue endboiling point, such as 370° C., including LPG, kerosene, naphtha, andatmospheric gas oil range components. The remaining bottoms fraction isthe unconverted oil fraction, all or a portion of which can beeffectively integrated as feed to the high olefinic fluid catalyticcracking zone 700 as described herein.

In certain embodiments, 0-100 wt % of the vacuum residue stream 168 canbe processed in a residue treatment center 800 (shown in dashed lines asan optional embodiment). In additional embodiments, 0-100 wt % of thepyrolysis oil from the steam cracker complex can be routed to theresidue treatment center 800. The residue treatment center 800 caninclude, but is not limited to, one or more of: a catalytic hydrogenaddition process, such as a residue hydrocracking system; a thermalcoking process, such as a delayed coker; and/or a solvent deasphaltingprocess. In certain embodiments, the residue treatment center 800produces one or more of a distillate fraction 808, a heavy fraction 806,and/or a bottoms fraction 804. The distillate fraction 808 can include,for instance, one or more middle distillate streams boiling in thetemperature range including and below atmospheric gas oil rangefractions (for instance in the temperature range of 36-370° C.), orincluding and below medium atmospheric gas oil range fractions. Notethat when the residue treatment center 800 is solvent deasphalting, adistillate fraction 808 is not produced. Portions of the distillatefraction 808 can be used as feed to the mixed feed steam cracking zone230, feed to one or more of the integrated hydroprocessing zones, and/orused for production of fuel components. All or a portion of the heavyfraction 806 can include, for instance, one or more streams of treatedheavy range hydrocarbons boiling above the atmospheric gas oil range(for instance 370° C.), or above the medium atmospheric gas oil range;or deasphalted oil in a solvent deasphalting unit. Portions of the heavyfraction 806 can be used as feed to the gas oil steam cracking zone 250,feed to one or more of the integrated hydroprocessing zones, recoveredas unconverted oil product, used for lube oil production in a base oilproduction zone, and/or incorporated in a fuel oil pool. The bottomsfraction 804 can include, for instance, pitch in a residue hydrocrackingsystem, petroleum coke in a delayed coker, or asphalt in a solventdeasphalting unit).

Embodiments of systems and processes incorporating certain vacuumresidue hydroprocessing zones are disclosed in U.S. patent applicationSer. No. 15/817,133 filed on Nov. 17, 2017, entitled “Process and Systemfor Conversion of Crude Oil to Petrochemicals and Fuel ProductsIntegrating Vacuum Residue Hydroprocessing,” and U.S. patent applicationSer. No. 15/817,136 filed on Nov. 17, 2017, entitled “Process and Systemfor Conversion of Crude Oil to Petrochemicals and Fuel ProductsIntegrating Vacuum Residue Conditioning and Base Oil Production,” whichare commonly owned and are incorporated by reference herein in theirentireties. Embodiments of systems and processes incorporating solventdeasphalting are disclosed in U.S. patent application Ser. No.15/817,140 filed on Nov. 17, 2017, entitled “Process and System forConversion of Crude Oil to Petrochemicals and Fuel Products IntegratingSolvent Deasphalting of Vacuum Residue,” which is commonly owned and isincorporated by reference herein in its entirety. Embodiments of systemsand processes incorporating thermal coking are disclosed in U.S. patentapplication Ser. No. 15/817,143 filed on Nov. 17, 2017, entitled“Process and System for Conversion of Crude Oil to Petrochemicals andFuel Products Integrating Delayed Coking of Vacuum Residue,” which iscommonly owned and is incorporated by reference herein in its entirety.

The hydrotreated gas oil fraction 304 is routed to the high olefinicfluid catalytic cracking zone 700. In certain embodiments, as shown indashed lines, the fourth middle distillate stream 130 is also routed thehigh olefinic fluid catalytic cracking zone 700, bypassing the vacuumgas oil hydrotreating zone 300. In certain embodiments, as shown indashed lines, the fourth middle distillate stream 130 is subjected tohydrotreating prior to passage to the high olefinic fluid catalyticcracking zone 700, for instance with the other feeds to the vacuum gasoil hydrotreating zone 300.

Products include fuel gas and LPG that are passed to an unsaturated gasplant 702, fluid catalytic cracking naphtha 706, which can be routed toa naphtha hydrotreating zone 670 as shown in FIG. 21; a light cycle oilstream 708, all or a portion of which is passed to the dieselhydrotreating zone 180, and a slurry oil or heavy cycle oil stream 710that can be routed to a fuel oil pool or used as feedstock forproduction of carbon black. In certain embodiments, all or a portion offluid catalytic cracking naphtha 706 can be routed to the aromaticsextraction zone 620 without hydrotreating. In certain embodiments, 0-100wt % 712 of the light cycle oil stream 708 is routed to a fuel oil pool

The unsaturated gas plant 702 and a high olefinic fluid catalyticcracking recovery section (not shown) are operated to recover a C2−stream 714 and a C3+ stream that are passed to an olefins recovery train270. In certain embodiments high olefinic fluid catalytic cracking lightends are selectively treated for removal of contaminants includingoxygen, nitrous oxides, nitriles, acetylene, methyl acetylene,butadiene, arsine, phosphine, stibine and mercury, while preservingethylene content. In certain embodiments treatment of the C2− off-gasstream includes use of a multi-functional catalyst as is known in theoperation of unsaturated gas plants before being passed to the olefinsrecovery train 270. Furthermore, a C3+ stream 716, generally containingC3s and C4s, is recovered from the high olefinic fluid catalyticcracking recovery section. In certain embodiments, this stream istreated in a mercaptan oxidation unit, as is known in the operation ofunsaturated gas plants, before routing to the to the olefins recoverytrain 270 or the steam cracking zone 230. In certain embodiments, theC3+ stream 716 stream is sent to a splitter, which can be integratedwith or separate from the olefins recovery train 270, to recoverolefins, and the remaining LPGs are routed to the mixed feed steamcracking zone 230. All, a substantial portion, a significant portion ora major portion of the C2− stream 714 and the C3+ stream 716 are routedthrough the unsaturated gas plant. The remainder, if any, can be routedto the mixed feed steam cracking zone 230 and/or the olefins recoverytrain 270.

In certain embodiments, the vacuum gas oil hydrotreating zone 300 can bebypassed and the high olefinic fluid catalytic cracking and associatedregenerator are operated to treat the products from the unit, includingflue gases produced in the catalyst regenerator, for control of sulfur.In other embodiments, the vacuum gas oil hydrotreating zone 300 isutilized, as treating the VGO reduces catalyst consumption in the higholefinic fluid catalytic cracking and enhances yield. In embodiments inwhich the vacuum gas oil hydrotreating zone 300 is utilized, flue gasdesulfurization of flue gases produced in the catalyst regenerator isalso provided.

As shown in FIGS. 12, 13 and 21, a portion of the cycle oil product fromthe high olefinic fluid catalytic cracking, cycle oil 708, is passed tothe diesel hydrotreating zone 180, and a portion of the cycle oilproduct from the high olefinic fluid catalytic cracking, cycle oil 712,is diverted, for instance, for inclusion in a fuel oil pool. A quantity(wt %) of 0-5, 0-10, 0-15, or 0-20 of cycle oil stream 708 is passed tothe diesel hydrotreating zone 180 and the remainder passed to a fuel oilpool. Slurry oil 710 is also recovered from the high olefinic fluidcatalytic cracking zone 700. This heavy product is an effectivefeedstock for carbon black production, or can be included in a fuel oilpool.

There are many commercially available systems for maximizing thepropylene production utilizing a fluid catalytic cracking unit. Asuitable high olefinic fluid catalytic cracking zone 700 can include,but is not limited to, systems based on technology commerciallyavailable from Axens, IFP Group Technologies, FR; Honeywell UOP, US; CNPetroleum & Chemical Corporation (Sinopec), CN; KBR, Inc, US; or ChicagoBridge & Iron Company N.V. (CB&I), NL.

The high olefinic fluid catalytic cracking zone 700 can have one or morerisers/reactors, a disengager/stripper and one or more regenerators. Ifplural reactors are implemented, propylene yield and selectivity can bemaximized.

In certain embodiments, a fluid catalytic cracking unit configured witha riser reactor is provided that operates under conditions that promoteformation of light olefins, particularly propylene, and that minimizelight olefin-consuming reactions including hydrogen-transfer reactions.FIG. 22 is a simplified schematic illustration of a riser fluidcatalytic cracking unit. A fluid catalytic cracking unit 720 includes ariser reactor. Fluid catalytic cracking unit 720 includes areactor/separator 724 having a riser portion 726, a reaction zone 728and a separation zone 730. Fluid catalytic cracking unit 720 alsoincludes a regeneration vessel 732 for regenerating spent catalyst. Acharge 722 is introduced to the reaction zone, in certain embodimentsaccompanied by steam or other suitable gas for atomization of the feed(not shown). The charge 722, in the integrated process hereinhydrotreated gas oil, optionally in combination with atmospheric gas oilsuch as heavy atmospheric gas oil, is admixed and intimately contactedwith an effective quantity of heated fresh or regenerated solid crackingcatalyst particles which are conveyed via a conduit 734 fromregeneration vessel 732. The feed mixture and the cracking catalyst arecontacted under conditions to form a suspension that is introduced intothe riser 726. In a continuous process, the mixture of cracking catalystand hydrocarbon feedstock proceed upward through the riser 726 intoreaction zone 728. In the riser 726 and reaction zone 728, the hotcracking catalyst particles catalytically crack relatively largehydrocarbon molecules by carbon-carbon bond cleavage.

During the reaction, as is conventional in fluid catalytic crackingoperations, the cracking catalysts become coked and hence access to theactive catalytic sites is limited or nonexistent. Reaction products areseparated from the coked catalyst using any suitable configuration knownin fluid catalytic cracking units, generally referred to as theseparation zone 730 in a fluid catalytic cracking unit 720, forinstance, located at the top of the reactor 724 above the reaction zone728. The separation zone can include any suitable apparatus known tothose of ordinary skill in the art such as, for example, cyclones. Thereaction product is withdrawn through conduit 736. Catalyst particlescontaining coke deposits from fluid cracking of the hydrocarbonfeedstock pass through a conduit 738 to regeneration zone 732.

In regeneration zone 732, the coked catalyst comes into contact with astream of oxygen-containing gas, such as pure oxygen or air, whichenters regeneration zone 732 via a conduit 740. The regeneration zone732 is operated in a configuration and under conditions that are knownin typical fluid catalytic cracking operations. For instance,regeneration zone 732 can operate as a fluidized bed to produceregeneration off-gas comprising combustion products which is dischargedthrough a conduit 742. The hot regenerated catalyst is transferred fromregeneration zone 732 through conduit 734 to the bottom portion of theriser 726 for admixture with the hydrocarbon feedstock and noted above.

In one embodiment, a suitable fluid catalytic cracking unit 720 can besimilar to that described in U.S. Pat. Nos. 7,312,370, 6,538,169, and5,326,465, the disclosures of which are incorporated herein by referencein their entireties. In general, the operating conditions for thereactor of a suitable riser fluid catalytic cracking unit 720 include:

a reaction temperature (° C.) of from about 480-650, 480-620, 480-600,500-650, 500-620, or 500-600;

a reaction pressure (barg) of from about 1-20, 1-10, or 1-3;

a contact time (in the reactor, seconds) of from about 0.5-10, 0.5-5,0.5-2, 1-10, 1-5, or 1-2; and

a catalyst-to-feed ratio of about 1:1 to 15:1, 1:1 to 10:1, 1:1 to 20:1,8:1 to 20:1, 8:1 to 15:1, or 8:1 to 10:1.

In certain embodiments, a fluid catalytic cracking unit configured witha downflow reactor is provided that operates under conditions thatpromote formation of light olefins, particularly propylene, and thatminimize light olefin-consuming reactions including hydrogen-transferreactions. FIG. 23 is a simplified schematic illustration of a downflowfluid catalytic cracking unit. A fluid catalytic cracking unit 760includes a reactor/separator 764 having a reaction zone 768 and aseparation zone 770. Fluid catalytic cracking unit 760 also includes aregeneration zone 772 for regenerating spent catalyst. In particular, acharge 762 is introduced to the reaction zone, in certain embodimentsaccompanied by steam or other suitable gas for atomization of the feed(not shown). An effective quantity of heated fresh or hot regeneratedsolid cracking catalyst particles from regeneration zone 772 is conveyedto the top of reaction zone 768 also transferred, for instance, througha downwardly directed conduit or pipe 774, commonly referred to as atransfer line or standpipe, to a withdrawal well or hopper (not shown)at the top of reaction zone 768. Hot catalyst flow is typically allowedto stabilize in order to be uniformly directed into the mix zone or feedinjection portion of reaction zone 768. The charge 762 is injected intoa mixing zone through feed injection nozzles typically situatedproximate to the point of introduction of the regenerated catalyst intoreaction zone 768. These multiple injection nozzles result in thethorough and uniform mixing of the hot catalyst and the charge 762, inthe integrated process herein hydrotreated gas oil, optionally incombination with atmospheric gas oil such as heavy atmospheric gas oil.Once the charge contacts the hot catalyst, cracking reactions occur.

The reaction vapor of hydrocarbon cracked products, unreacted feed andcatalyst mixture quickly flows through the remainder of reaction zone768 and into the rapid separation zone 770 at the bottom portion ofreactor/separator 764. Cracked and uncracked hydrocarbons are directedthrough a conduit or pipe 776 to a conventional product recovery sectionknown in the art to yield as fluid catalytic cracking products lightolefins, gasoline and cycle oil, with a maximized propylene yield. Ifnecessary for temperature control, a quench injection can be providednear the bottom of reaction zone 768 immediately before the separationzone 770. This quench injection quickly reduces or stops the crackingreactions and can be utilized for controlling cracking severity toachieve the product slate.

The reaction temperature, i.e., the outlet temperature of the downflowreactor, can be controlled by opening and closing a catalyst slide valve(not shown) that controls the flow of hot regenerated catalyst fromregeneration zone 772 into the top of reaction zone 768. The heatrequired for the endothermic cracking reaction is supplied by theregenerated catalyst. By changing the flow rate of the hot regeneratedcatalyst, the operating severity or cracking conditions can becontrolled to produce the desired product slate. A stripper 778 is alsoprovided for separating oil from the catalyst, which is transferred toregeneration zone 772. The catalyst from separation zone 770 flows tothe lower section of the stripper 778 that includes a catalyst strippingsection into which a suitable stripping gas, such as steam, isintroduced through streamline 780. The stripping section is typicallyprovided with several baffles or structured packing (not shown) overwhich the downwardly flowing catalyst 788 passes counter-currently tothe flowing stripping gas. The upwardly flowing stripping gas, which istypically steam, is used to “strip” or remove any additionalhydrocarbons that remain in the catalyst pores or between catalystparticles. The stripped and spent catalyst is transported by lift forcesfrom the combustion air stream 790 through a lift riser of theregeneration zone 770. This spent catalyst, which can also be contactedwith additional combustion air, undergoes controlled combustion of anyaccumulated coke. Flue gases are removed from the regenerator viaconduit 792. In the regenerator, the heat produced from the combustionof the by-product coke is transferred to the catalyst raising thetemperature required to provide heat for the endothermic crackingreaction in the reaction zone 768. According to the process herein,since the light solvent feedstock is combined with the heavy feedstockas the feed 762, the solvent to oil ratio in the initial solventdeasphalting/demetalizing process is selected so as to providesufficient coking of the catalyst to provide the heat balance duringregeneration.

In one embodiment, a suitable fluid catalytic cracking unit 760 with adownflow reactor that can be employed in the process described hereincan be similar to those described in U.S. Pat. No. 6,656,346, and USPatent Publication Number 2002/0195373, the disclosures of which areincorporated herein by reference in their entireties. Importantproperties of downflow reactors include introduction of feed at the topof the reactor with downward flow, shorter residence time as compared toriser reactors, and high catalyst-to-oil ratio, for instance, in therange of about 20:1 to about 30:1. In general, the operating conditionsfor the reactor of a suitable propylene production downflow fluidcatalytic cracking unit include

a reaction temperature (° C.) of from about 550-650, 550-630, 550-620,580-650, 580-630, 580-620, 590-650, 590-630, 590-620;

a reaction pressure (barg) of from about 1-20, 1-10, or 1-3;

a contact time (in the reactor, seconds) of from about 0.1-30, 0.1-10,0.1-0.7, 0.2-30, 0.2-10, or 0.2-0.7; and

a catalyst-to-feed ratio of about 1:1 to 40:1, 1:1 to 30:1, 10:1 to30:1, or 10:1 to 30:1.

The catalyst used in the process described herein can be conventionallyknown or future developed catalysts used in fluid catalytic crackingprocesses, such as zeolites, silica-alumina, carbon monoxide burningpromoter additives, bottoms cracking additives, light olefin-producingadditives and any other catalyst additives routinely used in the fluidcatalytic cracking process. In certain embodiments, suitable crackingzeolites in the fluid catalytic cracking process include zeolites Y,REY, USY, and RE-USY. For enhanced naphtha cracking potential, apreferred shaped selective catalyst additive can be employed, such asthose used in fluid catalytic cracking processes to produce lightolefins and increase fluid catalytic cracking gasoline octane is ZSM-5zeolite crystal or other pentasil type catalyst structure. This ZSM-5additive can be mixed with the cracking catalyst zeolites and matrixstructures in conventional fluid catalytic cracking catalyst and isparticularly suitable to maximize and optimize the cracking of the crudeoil fractions in the downflow reaction zones.

Fluid catalytic cracking naphtha 706 is also recovered from the higholefinic fluid catalytic cracking zone 700. In certain embodiments, asdepicted for instance in FIGS. 12, 13 and 21, fluid catalytic crackingnaphtha 706 is further treated in the naphtha hydrotreating zone 670 inthe presence of an effective amount of hydrogen obtained from recyclewithin the naphtha hydrotreating zone 670 and make-up hydrogen 674.Effluent fuel gas is recovered and, for instance, passed to a fuel gassystem. In certain embodiments, all or a portion of the make-up hydrogen674 is derived from the steam cracker hydrogen stream 210 from theolefins recovery train 270.

The cracked naphtha hydrotreating zone 670 operates under conditionseffective to ensure removal of substantially all nitrogen, sincenitrogen is a limiting contaminant in the aromatics extraction andsubsequent processes. Due to the high temperature conditions effectivefor nitrogen removal, saturation of aromatics occurs, for instance, inthe range of about 15% saturation, ahead of recovery. Effluents from thecracked naphtha hydrotreating zone 670 are a hydrotreated fluidcatalytic cracking naphtha stream 672, and fuel gas.

A suitable cracked naphtha hydrotreating zone 670 can include, but isnot limited to, systems based on technology commercially available fromHoneywell UOP, US; Chevron Lummus Global LLC (CLG), US; or Axens, IFPGroup Technologies, FR.

The effluent from the cracked naphtha hydrotreating reactor generallycontain C5-C9+ hydrocarbons. In certain embodiments, C5-C9+ hydrocarbonsare passed to the aromatics extraction zone 620, and the aromaticsextraction zone 620 includes a depentanizing step to remove CSs. Inother embodiments and as shown for instance in FIGS. 12 and 13, crackednaphtha hydrotreating zone 670 includes a depentanizing step to removeC5s, which are recycled as stream 676 to the mixed feed steam crackingzone 230. The hydrotreated fluid catalytic cracking naphtha stream 672,generally containing C6-C9+ hydrocarbons, is passed to the aromaticsextraction zone 620.

The fluid catalytic cracking naphtha hydrotreating zone 670 can containone or more fixed-bed, ebullated-bed, slurry-bed, moving bed, continuousstirred tank (CSTR) or tubular reactors, in series and/or parallelarrangement. Additional equipment, including exchangers, furnaces, feedpumps, quench pumps, and compressors to feed the reactor(s) and maintainproper operating conditions, are well known and are considered part ofthe fluid catalytic cracking naphtha hydrotreating zone 670. Inaddition, equipment, including pumps, compressors, high temperatureseparation vessels, low temperature separation vessels and the like toseparate reaction products and provide hydrogen recycle within the fluidcatalytic cracking naphtha hydrotreating zone 670, are well known andare considered part of the fluid catalytic cracking naphthahydrotreating zone 670.

The fluid catalytic cracking naphtha hydrotreating zone 670 is operatedunder conditions effective to treat fluid catalytic cracking naphtha toproduce hydrotreated naphtha 672 that can be used as additional feed tothe aromatics extraction zone 620 for recovery of BTX streams. Incertain embodiments hydrotreated naphtha 672 can be used for fuelproduction.

In certain embodiments, the cracked naphtha hydrotreating zone 670operating conditions include:

a reactor inlet temperature (° C.) in the range of from about 293-450,293-410, 293-391, 332-450, 332-410, 332-391, 352-450, 352-410, 352-391or 368-374;

a reactor outlet temperature (° C.) in the range of from about 316-482,316-441, 316-420, 357-482, 357-441, 357-420, 378-482, 378-441, 378-420or 396-404;

a start of run (SOR) reaction temperature (° C.), as a weighted averagebed temperature (WABT), in the range of from about 284-436, 284-398,284-379, 322-436, 322-398, 322-379, 341-436, 341-398, 341-379 or357-363;

an end of run (EOR) reaction temperature (° C.), as a WABT, in the rangeof from about 316-482, 316-441, 316-420, 357-482, 357-441, 357-420,378-482, 378-441, 378-420 or 396-404;

a reaction inlet pressure (barg) in the range of from about 44-66,44-60, 44-58, 49-66, 49-60, 49-58, 52-66, 52-60, 52-58 or 53-56;

a reaction outlet pressure (barg) in the range of from about 39-58,39-53, 39-51, 43-58, 43-53, 43-51, 46-58, 46-53 or 46-51;

a hydrogen partial pressure (barg) (outlet) in the range of from about22-33, 22-30, 22-29, 25-33, 25-30, 25-29, 26-33, 26-30 or 26-29;

a hydrogen treat gas feed rate (SLt/Lt) up to about 640, 620, 570 or542, in certain embodiments from about 413-620, 413-570, 413-542,465-620, 465-570, 465-542, 491-620, 491-570 or 491-542;

a hydrogen quench gas feed rate (SLt/Lt) up to about 95, 85, 78 or 75,in certain embodiments from about 57-85, 57-78, 57-75, 64-85, 64-78,64-75, 68-85, 68-78 or 68-75; and

a make-up hydrogen feed rate (SLt/Lt) up to about 120, 110 or 102, incertain embodiments from about 78-120, 78-110, 78-102, 87-120, 87-110,87-102, 92-120, 92-110, 92-102 or 95-100.

An effective quantity of hydrotreating catalyst is provided in the fluidcatalytic cracking naphtha hydrotreating zone 670, including thosepossessing hydrotreating functionality and which generally contain oneor more active metal component of metals or metal compounds (oxides orsulfides) selected from the Periodic Table of the Elements IUPAC Groups6-10. In certain embodiments, the active metal component is one or moreof Co, Ni, W and Mo. The active metal component is typically depositedor otherwise incorporated on a support, such as amorphous alumina,amorphous silica alumina, zeolites, or combinations thereof. In certainembodiments, the catalyst used in the fluid catalytic cracking naphthahydrotreating zone 670 includes one or more catalyst selected fromCo/Mo, Ni/Mo, Ni/W, and Co/Ni/Mo. Combinations of one or more of Co/Mo,Ni/Mo, Ni/W and Co/Ni/Mo, can also be used. The combinations can becomposed of different particles containing a single active metalspecies, or particles containing multiple active species. In certainembodiments, Co/Mo hydrodesulfurization catalyst is suitable. Effectiveliquid hourly space velocity values (h⁻¹), on a fresh feed basisrelative to the hydrotreating catalysts, are in the range of from about0.1-10.0, 0.1-5.0, 0.1-2.0, 0.3-10.0, 0.3-5.0, 0.3-2.0, 0.5-10.0,0.5-5.0, 0.5-2.0 or 0.8-1.2. Suitable hydrotreating catalysts used inthe fluid catalytic cracking naphtha hydrotreating zone 670 have anexpected lifetime in the range of about 28-44, 34-44, 28-38 or 34-38months.

The mixed feed steam cracking zone 230, which operates as high severityor low severity thermal cracking process, generally converts LPG,naphtha and heavier hydrocarbons primarily into a mixed product stream220 containing mixed C1-C4 paraffins and olefins. In certainembodiments, the mixed feed steam cracking zone 230 processesstraight-run liquids from the crude unit, propane (from outside batterylimits and/or recycled) and various recycle streams from chemicalproduction and recovery areas within the integrated process and system.A suitable mixed feed steam cracking zone 230 can include, but is notlimited to, systems based on technology commercially available fromLinde AG, DE; TechnipFMC plc, UK; Chicago Bridge & Iron Company N.V.(CB&I), NL; or KBR, Inc, US.

Plural feeds to the mixed feed steam cracking zone 230 include: lightends 152, light naphtha 138 and heavy naphtha 140 (or a full rangestraight run naphtha 136 as shown in other embodiments) from the crudecomplex 100; a LPG stream 634 from a transalkylation zone 630; a C3+stream 716 recovered from the high olefinic fluid catalytic crackingzone 700; a recycle stream 282 from the methyl acetylene/propadiene(MAPD) saturation and propylene recovery zone 280, described below; C4raffinate 524 from the 1-butene recovery zone 520 described below; C5sstream 676 from the fluid catalytic cracking naphtha hydrotreating(“FCCN HT”) zone 670; C5s stream 606 from the py-gas hydrotreating zone600; wild naphtha 184 from the diesel hydrotreating zone 180 describedabove (in certain embodiments via the crude complex); naphtha from thevacuum gas oil hydroprocessing zone described above (wild naphtha 326 orhydrotreated naphtha 306) described above (in certain embodiments viathe crude complex); a raffinate stream 646 from the aromatics extractionzone 620; in certain embodiments a C5 cut derived from the pyrolysisgasoline described below; and optionally, propane stream 228 (fromoutside battery limits). In certain embodiments, the mixed feed steamcracking zone 230 can accept alternate feeds from other sources, forinstance, other naphtha range feeds that may become available fromoutside of the battery limits.

The products from the mixed feed steam cracking zone 230 include aquenched cracked gas stream 220 containing mixed C1-C4 paraffins andolefins that is routed to the olefins recovery zone 270, a raw pyrolysisgasoline stream 212 that is routed to a py-gas hydrotreating zone 600 toprovide feed 604 to the aromatics extraction zone 620, and a pyrolysisfuel oil stream 218.

The mixed feed steam cracking zone 230 operates under parameterseffective to crack the feed into desired products including ethylene,propylene, butadiene, and mixed butenes. Pyrolysis gasoline andpyrolysis oil are also recovered. In certain embodiments, the steamcracking furnace(s) are operated at conditions effective to produce aneffluent having a propylene-to-ethylene weight ratio of from about0.3-0.8, 0.3-0.6, 0.4-0.8 or 0.4-0.6.

The mixed feed steam cracking zone 230 generally comprises one or moretrains of furnaces. For instance, a typical arrangement includesreactors that can operate based on well-known steam pyrolysis methods,that is, charging the thermal cracking feed to a convection section inthe presence of steam to raise the temperature of the feedstock, andpassing the heated feed to the pyrolysis reactor containing furnacetubes for cracking. In the convection section, the mixture is heated toa predetermined temperature, for example, using one or more waste heatstreams or other suitable heating arrangement.

The feed mixture is heated to a high temperature in a convection sectionand material with a boiling point below a predetermined temperature isvaporized. The heated mixture (in certain embodiments along withadditional steam) is passed to the pyrolysis section operating at afurther elevated temperature for short residence times, such as 1-2seconds or less, effectuating pyrolysis to produce a mixed productstream. In certain embodiments separate convection and radiant sectionsare used for different incoming feeds to the mixed feed steam crackingzone 230 with conditions in each optimized for the particular feed.

In certain embodiments, steam cracking in the mixed feed steam crackingzone 230 is carried out using the following conditions: a temperature (°C.) in the convection section in the range of about 400-600, 400-550,450-600 or 500-600; a pressure (barg) in the convection section in therange of about 4.3-4.8, 4.3-4.45, 4.3-4.6, 4.45-4.8, 4.45-4.6 or4.6-4.8; a temperature (° C.) in the pyrolysis section in the range ofabout 700-950, 700-900, 700-850, 750-950, 750-900 or 750-850; a pressure(barg) in the pyrolysis section in the range of about 1.0-1.4, 1.0-1.25,1.25-1.4, 1.0-1.15, 1.15-1.4 or 1.15-1.25; a steam-to-hydrocarbon ratioin the in the convection section in the range of about 0.3:1-2:1,0.3:1-1.5:1, 0.5:1-2:1, 0.5:1-1.5:1, 0.7:1-2:1, 0.7:1-1.5:1, 1:1-2:1 or1:1-1.5:1; and a residence time (seconds) in the pyrolysis section inthe range of about 0.05-1.2, 0.05-1, 0.1-1.2, 0.1-1, 0.2-1.2, 0.2-1,0.5-1.2 or 0.5-1.

In operation of the mixed feed steam cracking zone 230, effluent fromthe cracking furnaces is quenched, for instance, using transfer lineexchangers, and quenched in a quench tower. The light products, quenchedcracked gas stream 220, are routed to the olefins recovery zone 270.Heavier products are separated in a hot distillation section. A rawpyrolysis gasoline stream is recovered in the quench system. Pyrolysisoil 218 is separated at a primary fractionator tower before the quenchtower.

In operation of one embodiment of the mixed feed steam cracking zone230, the feedstocks are mixed with dilution steam to reduce hydrocarbonpartial pressure and then are preheated. The preheated feeds are fed toempty tubular reactors mounted in the radiant sections of the crackingfurnaces. The hydrocarbons undergo free-radical pyrolysis reactions toform light olefins ethylene and propylene, and other by-products. Incertain embodiments, dedicated cracking furnaces are provided withcracking tube geometries optimized for each of the main feedstock types,including ethane, propane, and butanes/naphtha. Less valuablehydrocarbons, such as ethane, propane, C4 raffinate, and aromaticsraffinate, produced within the integrated system and process, arerecycled to extinction in the mixed feed steam cracking zone 230.

In certain embodiments, cracked gas from the furnaces is cooled intransfer line exchangers (quench coolers), for example, producing 1800psig steam suitable as dilution steam. Quenched cracked gas enters aprimary fractionator associated with the mixed feed steam cracker 230that removes pyrolysis fuel oil bottoms from lighter components. Theprimary fractionator enables efficient recovery of pyrolysis fuel oil.Pyrolysis fuel oil is stripped with steam in a fuel oil stripper tocontrol product vapor pressure, and cooled. In addition, secondaryquench is carried out by direct injection of pyrolysis fuel oil asquench oil into liquid furnace effluents. The stripped and cooledpyrolysis fuel oil can be sent to a fuel oil pool or product storage.The primary fractionator overhead is sent to a quench water tower;condensed dilution steam for process water treating, and raw pyrolysisgasoline, are recovered. Quench water tower overhead is sent to theolefins recovery zone 270, particularly the first compression stage. Rawpyrolysis gasoline is sent to a gasoline stabilizer to remove any lightends and to control vapor pressure in downstream pyrolysis gasolineprocessing. A closed-loop dilution steam/process water system isenabled, in which dilution steam is generated using heat recovery fromthe primary fractionator quench pumparound loops. The primaryfractionator enables efficient recovery of pyrolysis fuel oil due toenergy integration and pyrolysis fuel oil content in the light fractionstream.

The mixed product stream 220 effluent from the mixed feed steam crackingzone 230 is routed to an olefins recovery zone 270. For instance, lightproducts from the quenching step, C4-, H2 and H2S, are contained in themixed product stream 220 that is routed to the olefins recovery zone270. Products include: hydrogen 210 that is used for recycle and/orpassed to users; fuel gas 208 that is passed to a fuel gas system;ethane 272 that is recycled to the mixed feed steam cracking zone 230;ethylene 202 that is recovered as product; a mixed C3 stream 286 that ispassed to a methyl acetylene/propadiene saturation and propylenerecovery zone 280; and a mixed C4 stream 206 that is passed to abutadiene extraction zone 500.

The olefins recovery zone 270 operates to produce on-specification lightolefin (ethylene and propylene) products from the mixed product stream220. For instance, cooled gas intermediate products from the steamcracker is fed to a cracked gas compressor, caustic wash zone, and oneor more separation trains for separating products by distillation. Incertain embodiments two trains are provided. The distillation trainincludes a cold distillation section, wherein lighter products such asmethane, hydrogen, ethylene, and ethane are separated in a cryogenicdistillation/separation operation. The mixed C2 stream from the steamcracker contains acetylenes that are hydrogenated to produce ethylene inan acetylene selective hydrogenation unit. This system can also includeethylene, propane and/or propylene refrigeration facilities to enablecryogenic distillation.

In one embodiment, the mixed product stream 220 effluent from the mixedfeed steam cracking zone 230 is passed through three to five stages ofcompression. Acid gases are removed with caustic in a caustic washtower. After an additional stage of compression and drying, lightcracked gases are chilled and routed to a depropanizer. In certainembodiments light cracked gases are chilled with a cascaded two-levelrefrigeration system (propylene, mixed binary refrigerant) for cryogenicseparation. A front-end depropanizer optimizes the chilling train anddemethanizer loading. The depropanizer separates C3 and lighter crackedgases as an overhead stream, with C4s and heavier hydrocarbons as thebottoms stream. The depropanizer bottoms are routed to the debutanizer,which recovers a crude C4s stream 206 and any trace pyrolysis gasoline,which can be routed to the py-gas hydrotreating zone 600 (not shown).

The depropanizer overhead passes through a series of acetyleneconversion reactors, and is then fed to the demethanizer chilling train,which separates a hydrogen-rich product via a hydrogen purificationsystem, such as pressure swing adsorption. Front-end acetylenehydrogenation is implemented to optimize temperature control, minimizegreen oil formation and simplify ethylene product recovery byeliminating a C2 splitter pasteurization section that is otherwisetypically included in product recovery. In addition, hydrogenpurification via pressure swing adsorption eliminates the need for amethanation reactor that is otherwise typically included in productrecovery.

The demethanizer recovers methane in the overhead for fuel gas, and C2and heavier gases in the demethanizer bottoms are routed to thedeethanizer. The deethanizer separates ethane and ethylene overheadwhich feeds a C2 splitter. The C2 splitter recovers ethylene product202, in certain embodiments polymer-grade ethylene product, in theoverhead. Ethane 272 from the C2 splitter bottoms is recycled to themixed feed steam cracking zone 230. Deethanizer bottoms contain C3s fromwhich propylene product 204, in certain embodiments polymer-gradepropylene product, is recovered as the overhead of a C3 splitter, withpropane 282 from the C3 splitter bottoms recycled to the mixed feedsteam cracking zone 230.

A methyl acetylene/propadiene (MAPD) saturation and propylene recoveryzone 280 is provided for selective hydrogenation to convert methylacetylene/propadiene, and to recover propylene from a mixed C3 stream286 from the olefins recovery zone 270. The mixed C3 286 from theolefins recovery zone 270 contains a sizeable quantity of propadiene andpropylene. The methyl acetylene/propadiene saturation and propylenerecovery zone 280 enables production of propylene 204, which can bepolymer-grade propylene in certain embodiments.

The methyl acetylene/propadiene saturation and propylene recovery zone280 receives hydrogen 284 and mixed C3 286 from the olefins recoveryzone 270. Products from the methyl acetylene/propadiene saturation andpropylene recovery zone 280 are propylene 204 which is recovered, andthe recycle C3 stream 282 that is routed to the steam cracking zone 230.In certain embodiments, hydrogen 284 to saturate methyl acetylene andpropadiene is derived from hydrogen 210 obtained from the olefinsrecovery zone 270.

A stream 206 containing a mixture of C4s, known as crude C4s, from theolefins recovery zone 270, is routed to a butadiene extraction zone 500to recover a high purity 1,3-butadiene product 502 from the mixed crudeC4s. In certain embodiments (not shown), a step of hydrogenation of themixed C4 before the butadiene extraction zone 500 can be integrated toremove acetylenic compounds, for instance, with a suitable catalytichydrogenation process using a fixed bed reactor. 1,3-butadiene 502 isrecovered from the hydrogenated mixed C4 stream by extractivedistillation using, for instance, n-methyl-pyrrolidone (NMP) ordimethylformamide (DMF) as solvent. The butadiene extraction zone 500also produces a raffinate stream 504 containing butane/butene, which ispassed to a methyl tertiary butyl ether zone 510.

In one embodiment, in operation of the butadiene extraction zone 500,the stream 206 is preheated and vaporized into a first extractivedistillation column, for instance having two sections. NMP or DMFsolvent separates the 1,3-butadiene from the other C4 componentscontained in stream 504. Rich solvent is flashed with vapor to a secondextractive distillation column that produces a high purity 1,3 butadienestream as an overhead product. Liquid solvent from the flash and thesecond distillation column bottoms are routed to a primary solventrecovery column. Bottoms liquid is circulated back to the extractor andoverhead liquid is passed to a secondary solvent recovery or solventpolishing column. Vapor overhead from the recovery columns combines withrecycle butadiene product into the bottom of the extractor to increaseconcentration of 1,3-butadiene. The 1,3-butadiene product 502 can bewater washed to remove any trace solvent. In certain embodiments, theproduct purity (wt %) is 97-99.8, 97.5-99.7 or 98-99.6 of 1,3-butadieneand 94-99, 94.5-98.5, or 95-98 of the 1,3-butadiene content (wt %) ofthe feed is recovered. In addition to the solvent such as DMF, additivechemicals are blended with the solvent to enhance butadiene recovery. Inaddition, the extractive distillation column and primary solventrecovery columns are reboiled using high pressure steam (for instance,600 psig) and circulating hot oil from the aromatics extraction zone 620as heat exchange fluid.

A methyl tertiary butyl ether zone 510 is integrated to produce methyltertiary butyl ether 514 and a second C4 raffinate 516 from the first C4raffinate stream 504. In certain embodiments C4 Raffinate 1 504 issubjected to selective hydrogenation to selectively hydrogenate anyremaining dienes and prior to reacting isobutenes with methanol toproduce methyl tertiary butyl ether.

Purity specifications for recovery of a 1-butene product stream 522necessitate that the level of isobutylene in the second C4 raffinate 516be reduced. In general, the first C4 raffinate stream 504 containingmixed butanes and butenes, and including isobutylene, is passed to themethyl tertiary butyl ether zone 510. Methanol 512 is also added, whichreacts with isobutylene and produces methyl tertiary butyl ether 514.For instance, methyl tertiary butyl ether product and methanol areseparated in a series of fractionators, and routed to a second reactionstage. Methanol is removed with water wash and a final fractionationstage. Recovered methanol is recycled to the fixed bed downflowdehydrogenation reactors. In certain embodiments described below withrespect to FIG. 24, additional isobutylene can be introduced to themethyl tertiary butyl ether zone 510, for instance, derived from ametathesis conversion unit.

In operation of one embodiment of the methyl tertiary butyl ether zone510, the raffinate stream 504, contains 35-45%, 37-42.5%, 38-41% or39-40% isobutylene by weight. This component is removed from the C4raffinate 516 to attain requisite purity specifications, for instance,greater than or equal to 98 wt % for the 1-butene product stream 522from the C4 distillation unit 520. Methanol 512, in certain embodimentshigh purity methanol having a purity level of greater than or equal to98 wt % from outside battery limits, and the isobutylene contained inthe raffinate stream 504 and in certain embodiments isobutylene 544 frommetathesis (shown in dashed lines as an optional feed), react in aprimary reactor. In certain embodiments the primary reactor is a fixedbed downflow dehydrogenation reactor and operates for isobutyleneconversion in the range of about 70-95%, 75-95%, 85-95% or 90-95% on aweight basis. Effluent from the primary reactor is routed to a reactioncolumn where reactions are completed. In certain embodiments, exothermicheat of the reaction column and the primary reactor can optionally beused to supplement the column reboiler along with provided steam. Thereaction column bottoms contains methyl tertiary butyl ether, traceamounts, for instance, less than 2%, of unreacted methanol, and heavyproducts produced in the primary reactor and reaction column. Reactioncolumn overhead contains unreacted methanol and non-reactive C4raffinate. This stream is water washed to remove unreacted methanol andis passed to the 1-butene recovery zone 520 as the C4 raffinate 516.Recovered methanol is removed from the wash water in a methanol recoverycolumn and recycled to the primary reactor.

The C4 raffinate stream 516 from the methyl tertiary butyl ether zone510 is passed to the C4 distillation unit 520 for butene-1 recovery. Incertain embodiments, upstream of the methyl tertiary butyl ether zone510, or between the methyl tertiary butyl ether zone 510 and separationzone 520 for butene-1 recovery, a selective hydrogenation zone can alsobe included (not shown). For instance, in certain embodiments, raffinatefrom the methyl tertiary butyl ether zone 510 is selectivelyhydrogenated in a selective hydrogenation unit to produce butene-1.Other co-monomers and paraffins are also co-produced. The selectivehydrogenation zone operates in the presence of an effective amount ofhydrogen obtained from recycle within the selective hydrogenation zoneand make-up hydrogen; in certain embodiments, all or a portion of themake-up hydrogen for the selective hydrogenation zone is derived fromthe steam cracker hydrogen stream 210 from the olefins recovery train270. For instance, a suitable selective hydrogenation zone can include,but is not limited to, systems based on technology commerciallyavailable from Axens, IFP Group Technologies, FR; Haldor Topsoe A/S, DK;Clariant International Ltd, CH; Chicago Bridge & Iron Company N.V.(CB&I), NL; Honeywell UOP, US; or Shell Global Solutions, US.

For selective recovery of a 1-butene product stream 522 and a recyclestream 524 that is routed to the mixed feed steam cracking zone 230,and/or in certain embodiments described herein routed to a metathesiszone, one or more separation steps are used. For example, 1-butene canbe recovered using two separation columns, where the first columnrecovers olefins from the paraffins and the second column separates1-butene from the mixture including 2-butene, which is blended with theparaffins from the first column and recycled to the steam cracker as arecycle stream 524.

In certain embodiments, the C4 raffinate stream 516 from the methyltertiary butyl ether zone 510 is passed to a first splitter, from whichfrom isobutane, 1-butene, and n-butane are separated from heavier C4components. Isobutane, 1-butene, and n-butane are recovered as overhead,condensed in an air cooler and sent to a second splitter. Bottoms fromthe first splitter, which contains primarily cis- and trans-2-butene canbe added to the recycle stream 524, or in certain embodiments describedherein passed to a metathesis unit. In certain arrangements, the firstsplitter overhead enters the mid-point of the second splitter. Isobutaneproduct 526 can optionally be recovered in the overhead (shown in dashedlines), 1-butene product 522 is recovered as a sidecut, and n-butane isrecovered as the bottoms stream. Bottoms from both splitters isrecovered as all or a portion of the recycle stream 524.

The raw pyrolysis gasoline stream 212 from the steam cracker is treatedand separated into treated naphtha and other fractions. In certainembodiments, all, a substantial portion or a significant portion of thepyrolysis gasoline 212 from the steam cracking zone 230 is passed to thepy-gas hydrotreating zone 600. The raw pyrolysis gasoline stream 212 isprocessed in a py-gas hydrotreating zone 600 in the presence of aneffective amount of hydrogen obtained from recycle within the obtainedfrom recycle within and make-up hydrogen 602. Effluent fuel gas isrecovered and, for instance, passed to a fuel gas system. In certainembodiments, all or a portion of the make-up hydrogen 602 is derivedfrom the steam cracker hydrogen stream 210 from the olefins recoverytrain 270. For instance, a suitable py-gas hydrotreating zone 600 caninclude, but is not limited to, systems based on technology commerciallyavailable from Honeywell UOP, US; Chevron Lummus Global LLC (CLG), US;Axens, IFP Group Technologies, FR; Haldor Topsoe A/S, DK; or ChicagoBridge & Iron Company N.V. (CB&I), NL.

The py-gas hydrotreating zone 600 is operated under conditions, andutilizes catalyst(s), that can be varied over a relatively wide range.These conditions and catalyst(s) are selected for effectivehydrogenation for saturation of certain olefin and diolefin compounds,and if necessary for hydrotreating to remove sulfur and/or nitrogencontaining compounds. In certain embodiments, this is carried out in atleast two catalytic stages, although other reactor configurations can beutilized. Accordingly, py-gas hydrotreating zone 600 subjects thepyrolysis gasoline stream 212 to hydrogenation to produce hydrotreatedpyrolysis gasoline 604 effective as feed to the aromatics extractionzone 620. Effluent off-gases are recovered from the py-gas hydrotreatingzone 600 and are passed to the olefins recovery train, the saturated gasplant as part of the other gases stream 156, and/or directly to a fuelgas system. Liquefied petroleum gas can be recovered from the py-gashydrotreating zone 600 and routed to the mixed feed steam cracking zone,the olefins recovery train and/or the saturated gas plant.

In the py-gas hydrotreating zone 600, diolefins in the feed and olefinsin the C6+ portion of the feed are saturated to produce a naphtha stream604, a C5+ feed to the aromatics extraction zone. In certainembodiments, a depentanizing step associated with the py-gashydrotreating zone 600 separates all or a portion of the C5s, forinstance, as additional feed 606 to the mixed feed steam cracking zone230 and/or as feed to a metathesis unit 530 (as shown, for instance, inFIG. 6, 8 or 24). In other embodiments, a depentanizing step associatedwith the aromatics extraction zone 620 separates all or a portion of theC5s from the hydrotreated naphtha stream 604, for instance, asadditional feed to the mixed feed steam cracking zone 230 and/or as feedto a metathesis unit 530.

In certain embodiments, pyrolysis gasoline is processed in a firstreaction stage for hydrogenation and stabilization. Diolefins aresaturated selectively in the first reaction stage, and remaining olefinsare saturated in the second reaction stage along with converting feedsulfur into hydrogen sulfide. The pyrolysis gasoline can be treated in acold hydrotreating unit, therefore reducing the level of aromaticssaturation.

In an example of an effective py-gas hydrotreating zone 600, rawpyrolysis gasoline is passed through a coalescer before entering a feedsurge drum. The first stage reactor operates in mixed phase andselectively hydrogenates diolefins to mono-olefins and unsaturatedaromatics to side-chain saturated aromatics. Pd-based catalyst materialsare effective. Two parallel first-stage reactors can be used in certainembodiments to allow for regeneration in a continuous process withoutshutdown. In certain embodiments, the first-stage reactor contains threecatalyst beds with cooled first stage separator liquid recycled asquench material between each bed. First-stage effluent is stabilized andseparated in a column operating under slight vacuum to reducetemperature. In certain embodiments C5 from the C6+ is drawn, followedby a deoctanizer to remove C9+ and produce a C6-C8 heart naphtha cut.The column operates under slight vacuum to limit temperature. The firststage product is stripped to remove hydrogen, H₂S, and other light ends.In certain embodiments, the stripped first stage product is depentanizedto remove cracked C5, for instance, as feed to a metathesis unit. Asecond stage reactor operates in vapor phase and removes sulfur andsaturates olefins. The second stage product is stripped to removehydrogen, H₂S, and other light ends. In certain embodiments, bothreactors are multi-bed and use product recycle to control reactortemperature rise.

In certain embodiments, the first reaction stage of the py-gashydrotreating zone 600 operating conditions include:

a reactor inlet temperature (° C.) in the range of from about 80-135,80-125, 80-115, 95-135, 95-125, 95-115, 100-135, 100-125, 100-115 or107-111;

a reactor outlet temperature (° C.) in the range of from about 145-230,145-206, 145-200, 165-230, 165-206, 165-200, 175-230, 175-206, 175-200or 184-188;

a start of run (SOR) reaction temperature (° C.), as a weighted averagebed temperature (WABT), in the range of from about 75-125, 75-115,75-110, 90-125, 90-115, 90-110, 95-125, 95-115, 95-110 or 99-104;

an end of run (EOR) reaction temperature (° C.), as a WABT, in the rangeof from about 124-195, 124-180, 124-170, 140-195, 140-180, 140-170,150-195, 150-180, 150-170 or 158-163;

a reaction inlet pressure (barg) in the range of from about 25-40,25-35, 25-33, 28-40, 28-35, 28-33, 30-40, 30-35 or 30-33;

a reaction outlet pressure (barg) in the range of from about 23-35,23-33, 23-31, 25-35, 25-33, 25-31, 28-35, 28-33 or −28-31;

a hydrogen partial pressure (barg) (outlet) in the range of from about15-25, 15-22, 15-21, 18-25, 18-22, 18-21, 19-25 or 19-22;

a hydrogen treat gas feed rate (SLt/Lt) up to about 180, 165 or 156, incertain embodiments from about 120-180, 120-165, 120-156, 134-180,134-165, 134-156, 140-180, 140-165 or 140-156;

a liquid quench feed ratio (Lt quench/Lt feed) up to about 0.8, 0.7, 0.6or 0.5, and in certain embodiments in the range of from about 0.35-0.6,0.35-0.55, 0.35-0.5, 0.4-0.6, 0.4-0.55, 0.4-0.5, 0.45-0.6, 0.45-0.55 or0.45-0.5; and

a make-up hydrogen feed rate (SLt/Lt) up to about 60, 55, 47 or 45, incertain embodiments from about 34-55, 34-47, 34-45, 40-55, 40-47, 40-45,42-55, 42-47 or 42-45.

In certain embodiments, the second reaction stage of the py-gashydrotreating zone 600 operating conditions include:

a reactor inlet temperature (° C.) in the range of from about 225-350,225-318, 225-303, 255-350, 255-318, 255-303, 270-350, 270-318, 270-303or 285-291;

a reactor outlet temperature (° C.) in the range of from about 289-445,289-405, 289-386, 328-445, 328-405, 328-386, 345-445, 345-405, 345-386or 364-370;

a start of run (SOR) reaction temperature (° C.), as a weighted averagebed temperature (WABT), in the range of from about 217-336, 217-306,217-291, 245-336, 245-306, 245-291, 260-336, 260-306, 260-291 or274-280;

an end of run (EOR) reaction temperature (° C.), as a WABT, in the rangeof from about 325-416, 325-380, 325-362, 305-416, 305-380, 305-362,325-416, 325-380, 325-362 or 340-346;

a reaction inlet pressure (barg) in the range of from about 25-37,25-34, 25-32, 28-37, 28-34, 28-32, 29-37, 29-34 or 29-32;

a reaction outlet pressure (barg) in the range of from about 23-35,23-32, 23-30, 26-35, 26-32, 26-30, 28-35, 28-32 or 28-30;

a hydrogen partial pressure (barg) (outlet) in the range of from about6-10, 6-9, 7-10 or 7-9;

a hydrogen treat gas feed rate (SLt/Lt) up to about 135, 126, 116 or110, in certain embodiments from about 84-126, 84-116, 84-110, 95-126,95-116, 95-110, 100-126, 100-116 or 100-110; and

a make-up hydrogen feed rate (SLt/Lt) up to about 30, 27 or 24, incertain embodiments from about 18-30, 18-27, 18-24, 21-30, 21-27, 21-24,22-30, 22-27 or 22-24.

An effective quantity of catalyst possessing selective hydrogenationfunctionality is provided, which generally contain one or more activemetal component of metals or metal compounds (oxides or sulfides)selected from Co, Mo, Pt, Pd, Fe, or Ni. The active metal component istypically deposited or otherwise incorporated on a support, such asamorphous alumina, amorphous silica alumina, zeolites, or combinationsthereof. Exemplary selective hydrogenation catalyst predominantly use Pdas the active metal component on alumina support, including thosecommercially available under the trade name Olemax® 600 and Olemax® 601.Effective liquid hourly space velocity values (h⁻¹), on a fresh feedbasis relative to the first stage pyrolysis gasoline reactor catalyst,are in the range of from about 0.1-10.0, 0.1-5.0, 0.1-2.0, 0.3-10.0,0.3-5.0, 0.3-2.0, 0.5-10.0, 0.5-5.0, 0.5-2.0 or 0.9 to 1.44. Suitablecatalysts used in the first stage pyrolysis gasoline reactor have anexpected lifetime in the range of about 18-30, 22-30, 18-26 or 22-26months.

An effective quantity of second stage pyrolysis gasoline reactorcatalyst is provided, including those having hydrogenation functionalityand which generally contain one or more active metal component of metalsor metal compounds (oxides or sulfides) selected from the Periodic Tableof the Elements IUPAC Groups 6-10. In certain embodiments, the activemetal component is one or more of Co, Ni, W and Mo. The active metalcomponent is typically deposited or otherwise incorporated on a support,such as amorphous alumina, amorphous silica alumina, zeolites, orcombinations thereof. In certain embodiments, the catalyst used in thefirst stage pyrolysis gasoline reactor includes one or more catalystselected from Co/Mo, Ni/Mo, Ni/W, and Co/Ni/Mo. Combinations of one ormore of Co/Mo, Ni/Mo, Ni/W and Co/Ni/Mo, can also be used. For example,a combination of catalyst particles commercially available under thetrade names Olemax® 806 and Olemax® 807 can be used, with active metalcomponents of Co and Ni/Mo. The combinations can be composed ofdifferent particles containing a single active metal species, orparticles containing multiple active species. Effective liquid hourlyspace velocity values (h⁻¹), on a fresh feed basis relative to the firststage pyrolysis gasoline reactor catalyst, are in the range of fromabout 0.1-10.0, 0.1-5.0, 0.1-2.0, 0.3-10.0, 0.3-5.0, 0.3-2.0, 0.5-10.0,0.5-5.0, 0.5-2.0 or 0.8-1.2. Suitable catalysts used in the second stagepyrolysis gasoline reactor have an expected lifetime in the range ofabout 18-30, 22-30, 18-26 or 22-26 months.

Hydrotreated pyrolysis gasoline 604, hydrotreated fluid catalyticcracking naphtha 672, and all or a portion of the chemical richreformate stream 426, are routed to the aromatics extraction zone 620.As noted above, the chemical rich reformate stream 426 can be used invarying quantities as feed to the aromatics extraction zone 620. Incertain embodiments to maximize production of petrochemicals, all, asubstantial portion or a significant portion of the hydrotreatedpyrolysis gasoline 604 is passed to the aromatics extraction zone 620.In modes of operation in which production of gasoline is the objectivesome of the hydrotreated pyrolysis gasoline 604 is passed to a gasolinepool (not shown).

The aromatics extraction zone 620 includes, for instance, one or moreextractive distillation units, and operates to separate the hydrotreatedpyrolysis gasoline and fluid catalytic cracking naphtha into high-puritybenzene, toluene, xylenes and C9 aromatics. As depicted in FIG. 21, abenzene stream 624, a mixed xylenes stream 626 and a raffinate stream646 are recovered from the aromatics extraction zone 620, with theraffinate stream 646 routed to the mixed feed steam cracking zone 230 asadditional feed. In addition, a toluene stream 636 is passed from thearomatics extraction zone 620 to a toluene and C9+ transalkylation zone630 for production of additional benzene and xylenes, recycled as stream640 to the aromatics extraction zone 620. In certain embodimentsethylbenzene can be recovered (not shown). Heavy aromatics 642 are alsorecovered from the aromatics extraction zone 620.

In certain embodiments of operation of the aromatics extraction zone620, aromatics are separated from the feed by extractive distillationusing, for instance, n-formylmorpholine (NFM), as an extractive solvent.Benzene, toluene, mixed xylenes and C9+ aromatics are separated viadistillation. Benzene and mixed xylenes are recovered as product streams624 and 626, and toluene 636 and C9+ aromatics 638 are sent to thetoluene and C9+ transalkylation zone 630. The transalkylation zoneproduct stream 640 containing benzene and mixed xylenes is returned tothe recovery section of the aromatics extraction zone 620. A paraffinicraffinate stream 646 is recycled as feed to the mixed feed steamcracking zone 230. In certain embodiments, the paraffinic raffinatestream 646 is in direct fluid communication with the mixed feed steamcracking zone 230, that is, the stream is not subject to furthercatalytic processing prior to the steam cracking step.

Selection of solvent, operating conditions, and the mechanism ofcontacting the solvent and feed permit control over the level ofaromatic extraction. For instance, suitable solvents includen-formylmorpholine, furfural, N-methyl-2-pyrrolidone, dimethylformamide,dimethylsulfoxide, phenol, nitrobenzene, sulfolanes, acetonitrile, orglycols, and can be provided in a solvent to oil ratio of up to about20:1, in certain embodiments up to about 4:1, and in further embodimentsup to about 2:1. Suitable glycols include diethylene glycol, ethyleneglycol, triethylene glycol, tetraethylene glycol and dipropylene glycol.The extraction solvent can be a pure glycol or a glycol diluted withfrom about 2-10 wt % water. Suitable sulfolanes includehydrocarbon-substituted sulfolanes (e.g., 3-methyl sulfolane), hydroxysulfolanes (e.g., 3-sulfolanol and 3-methyl-4-sulfolanol), sulfolanylethers (e.g., methyl-3-sulfolanyl ether), and sulfolanyl esters (e.g.,3-sulfolanyl acetate).

The aromatic separation apparatus can operate at a temperature in therange of from about 40-200, 40-150, 60-200, 60-150, 86-200 or 80-150° C.The operating pressure of the aromatic separation apparatus can be inthe range of from about 1-20, 1-16, 3-20, 3-16, 5-20 or 5-16 barg. Typesof apparatus useful as the aromatic separation apparatus in certainembodiments of the system and process described herein includeextractive distillation columns.

In one embodiment of operation of the aromatics extraction zone 620, thefeed contains primarily C6+ components, and is fractionated into a“heart cut” of C6-C8, a heavy C9+ fraction. The C6-C8 cut is routed tothe extractive distillation system where aromatics are separated fromnon-aromatics (saturates) via solvent distillation. The raffinate(non-aromatics) from the C6-C8 is removed and recycled back to thecracking complex as a feedstock. The aromatics are soluble in thesolvent and are carried from the bottom of the extractive distillationcolumn to the solvent stripper where they are stripped from the solventto produce aromatics extract and lean solvent which is recycled back tothe extractive distillation column. The mixed aromatics extract isrouted to a series of fractionation columns (a benzene column, a toluenecolumn and a xylene column) where each aromatic species is successivelyremoved, for instance, as benzene stream 624 and mixed xylenes stream626. The heavy C9+ fraction is further separated into C9 and C10+material. The toluene and C9 products are routed to the toluene and C9+transalkylation zone 630 where they are reacted to form additionalbenzene and mixed xylenes. This stream is recycled back to thefractionation portion of the aromatics extraction zone 620 to recoverthe benzene and mixed xylenes as well as to recycle the unconvertedtoluene and C9 aromatics. The transalkylation effluent does not requirere-extraction in the solvent distillation section and therefore isrouted to the inlet of the benzene column. In certain embodimentstoluene can be recycled to extinction, or approaching extinction. C10and heavier aromatics are removed as product 642. In certainembodiments, ethylbenzene can be recovered.

The toluene and C9+ transalkylation zone 630 operates under conditionseffective to disproportionate toluene and C9+ aromatics into a mixedstream 640 containing benzene, mixed xylenes and heavy aromatics.Product ratio of benzene and xylene can be adjusted by selection ofcatalyst, feedstock and operating conditions. The transalkylation zone630 receives as feed the toluene stream 636 and the C9+ aromatics stream638 from the aromatics extraction zone 620. A small quantity of hydrogen632, in certain embodiments which is obtained all or in part from thehydrogen stream 210 derived from the olefins recovery zone 270, issupplied for transalkylation reactions. Side cracking reactions occurproducing fuel gas stream, for instance, passed to the fuel gas system,and LPG stream 634 that is recycled to mixed feed steam cracking zone. Asmall amount, such as 0.5-3 wt % of the total feed to the aromaticsextraction, of heavy aromatics are produced due to condensationreactions and are passed to the mixed stream 640 for recovery with otherheavy aromatics.

In operation of one embodiment of the toluene and C9+ transalkylationzone 630, toluene and C9 aromatics are reacted with hydrogen under mildconditions to form a mixture of C6-C11 aromatics. The mixed aromaticproduct stream 640 is recycled back to the aromatics extraction zone 620where the benzene and mixed xylenes are recovered as products. C7 and C9aromatics are recycled back as feed to the transalkylation zone 630, andthe C10+ fraction is removed from the aromatics extraction zone 620 asheavy aromatics stream 642. The disproportionation reactions occur inthe presence of an effective quantity of hydrogen. Minimal amounts ofhydrogen is consumed by cracking reactions under reactor conditions.Purge gas is recycled back to the cracking complex for componentrecovery.

In certain embodiments, pyrolysis oil streams 236 and 256 can be blendedinto the fuel oil pool as a low sulfur component, and/or used as carbonblack feedstock. In additional embodiments, either or both of thepyrolysis oil streams 236 and 256 can be fractioned (not shown) intolight pyrolysis oil and heavy pyrolysis oil. For instance, lightpyrolysis oil can be blended with one or more of the middle distillatestreams, so that 0-100% of light pyrolysis oil derived from either orboth of the pyrolysis oil streams 236 and 256 is processed to producediesel fuel product and/or additional feed to the mixed feed steamcracking zone 230. In another embodiment 0-100% of light pyrolysis oilderived from either or both of the pyrolysis oil streams 236, 256 can beprocessed in the vacuum gas oil hydroprocessing zone. In certainembodiments, all, a substantial portion, a significant portion or amajor portion of light pyrolysis oil can be passed to one or both of thediesel hydrotreating zone 180 and/or the vacuum gas oil hydroprocessingzone; any remainder can be blended into the fuel oil pool. Heavypyrolysis oil can be blended into the fuel oil pool as a low sulfurcomponent, and/or used as a carbon black feedstock. In furtherembodiments, 0-100% of light pyrolysis oil and/or 0-100% of heavypyrolysis oil derived from either or both of the pyrolysis oil streams236, 256 can be processed in the optional residue treating zone 800. Incertain embodiments, all, a substantial portion, a significant portionor a major portion of the pyrolysis oil streams 236, 256 (light andheavy) can be processed in the optional residue treating zone 800.

FIG. 24 depicts a variation to any of the above described processes,including integration of a metathesis unit 530. For instance, a suitablemetathesis zone 530 can include, but is not limited to, systems based ontechnology commercially available from Chicago Bridge & Iron CompanyN.V. (CB&I), NL.

Feedstocks to the metathesis unit 530 include: a portion 536 of theethylene mixed feed steam cracking product; a C4 raffinate 3 stream 532from the C4 distillation unit 520, and an olefinic C5 cut 606 from thepy-gas hydrotreating zone 600. The C4 Raffinate-3 stream 532 is 0-100%of the total C4 Raffinate-3 from the 1-butene recovery zone 520; anyremaining portion 524 can be recycled to the mixed feed steam crackingzone 230. Products from the metathesis unit 530 include propylene 534and a stream 542, having a mixture of mostly saturated C4/C5 from ametathesis unit that is recycled to the mixed feed steam cracking zone.In certain embodiments, isobutylene 544 can also be recovered (shown indashed lines) and routed to the methyl tertiary butyl ether zone 510. Inembodiments that operate without separation of isobutylene, it isincluded within stream 542.

FIG. 25 depicts an embodiment in which fluid catalytic cracking naphtha706 and the raw pyrolysis gasoline stream 212 from the steam cracker arecommingled and processed in a naphtha hydrotreating zone 610. Thenaphtha hydrotreating zone 610 operates in the presence of an effectiveamount of hydrogen obtained from recycle within the naphthahydrotreating zone 610 and make-up hydrogen 680. In certain embodiments,all or a portion of the make-up hydrogen 680 is derived from the steamcracker hydrogen stream 210 from the olefins recovery train 270.Effluent fuel gas is recovered and, for instance, passed to a fuel gassystem.

The effluent from the cracked naphtha hydrotreating reactor generallycontain C5-C9+ hydrocarbons. In certain embodiments, C5-C9+ hydrocarbonsare passed to the aromatics extraction zone 620, and the aromaticsextraction zone 620 includes a depentanizing step to remove CSs. Inother embodiments and as shown for instance in FIG. 25, naphthahydrotreating zone 610 includes a depentanizing step to remove C5s,which are recycled as stream 644 to the mixed feed steam cracking zone230. The hydrotreated mixed naphtha stream 678, generally containingC6-C9+ hydrocarbons, is passed to the aromatics extraction zone 620. Theprocess of FIG. 25 operates according to the description with respect toFIGS. 12, 13 and 21, or any of the other embodiments herein, in allother aspects.

FIG. 26 depicts an embodiment in which kerosene sweetening is in anoptional unit, that is, the first middle distillate fraction 118 can berouted either through the kerosene sweetening zone 170 or routed to thedistillate hydrotreating zone 180. The process of FIG. 27 operatesaccording to the description with respect to FIGS. 12, 13 and 21, or anyof the other embodiments herein, in all other aspects.

During periods in which maximizing the kerosene fuel 172 is desired, thefirst middle distillate fraction 118 can be routed to the kerosenesweetening zone 170. During periods in which the feedstock to the mixedfeed steam cracking zone 230 is to be maximized, the first middledistillate fraction 118 can be routed to the distillate hydrotreatingzone 180, so as to produce additional hydrotreated naphtha 184. Inadditional alternative embodiments, the first middle distillate fraction118 can be divided (on a volume or weight basis, for example, with adiverter) so that a portion is passed to the distillate hydrotreatingzone 180 and the remaining portion is passed to the kerosene sweeteningzone 170.

FIG. 27 depicts an embodiment in which kerosene sweetening iseliminated. Accordingly, in the embodiment of FIG. 27 two middledistillate fractions are used. In this embodiment, a first middledistillate fraction 124 is routed to the distillate hydrotreating zone180, and a second middle distillate fraction 134 may be similar to thethird middle distillate fraction 126 described in other embodimentsherein. In one example using the arrangement shown in 27, the firstmiddle distillate fraction 124 contains kerosene range hydrocarbons andmedium AGO range hydrocarbons, and the second atmospheric distillationzone middle distillate fraction 134 contains heavy AGO rangehydrocarbons. In another example using the arrangement shown in FIG. 27,the first middle distillate fraction 124 contains kerosene rangehydrocarbons and a portion of medium AGO range hydrocarbons and thesecond middle distillate fraction 134 contains a portion of medium AGOrange hydrocarbons and heavy AGO range hydrocarbons. The process of FIG.27 operates according to the description with respect to FIGS. 9 and 11,or any of the other embodiments herein, in all other aspects.

Advantageously, process dynamics of the configurations and theintegration of units and streams attain a very high level of integrationof utility streams between the mixed feed steam cracking and otherprocess units, result in increased efficiencies and reduced overalloperating costs. For instance, the hydrogen can be tightly integrated sothat the net hydrogen demand from outside of the battery limits isminimized or even eliminated. In certain embodiments, the overallhydrogen utilization from outside of the battery limits is less thanabout 40, 30, 15, 10 or 5 wt % hydrogen based on the total hydrogenrequired by the hydrogen users in the integrated process. Hydrogen isrecovered from the olefins recovery train and the chemical reformer, andis supplied to the hydrogen users in the system, including the dieselhydrotreater, the gas oil hydrotreater or hydrocracker, the py-gashydrotreater, the fluid catalytic cracking naphtha hydrotreater, andtransalkylation, so as to derive most or all of the utility hydrogenfrom within the battery limits. In certain embodiments, there is zeroexternal hydrogen use, in which make-up hydrogen is only required toinitiate the operation, so that when the reactions reach equilibrium,the hydrogen derived from the mixed feed steam cracking productsprovides sufficient hydrogen to maintain the hydrogen requirements ofthe hydrogen users in the integrated process. In further embodiments,there is a net hydrogen gain, so that hydrogen can be added, forinstance, to the fuel gas that is used to operate the various heatingunits within the integrated process.

Furthermore, the integrated process described herein offers usefuloutlets for the off-gases and light ends from the hydroprocessing units.For instance, the stream 156 that is passed to the saturated gas plant150 of the crude complex 100 can contain off-gases and light ends fromthe hydroprocessing units, such as the diesel hydrotreating zone 180,the gas oil hydrotreating zone 300 and/or from the py-gas hydrotreatingzone 600. In other embodiments, in combination with or as an alternativeto the passing these off-gases and light ends to stream 156, all or aportion can be routed to the mixed feed steam cracking unit 230. Forinstance, C2s can be separated from the mixture of methane, hydrogen andC2s using a cold distillation section (“cold box”) including cryogenicdistillation/separation operations, which can be integrated with any orall of the mixed feed steam cracking unit 230, the saturated gas plant150 and/or the olefins recovery zone 270. Methane and hydrogen can bepassed to a fuel gas system or to an appropriate section of the olefinsrecovery zone 270, such as the hydrogen purification system. In stillfurther embodiments, in combination with or as an alternative to thepassing these off-gases and light ends to stream 156 and/or routing themto the mixed feed steam cracking unit 230, all or a portion can berouted to an appropriate section of the olefins recovery zone 270, suchas the depropanizer, or combining the gases with the depropanizeroverheads.

Embodiments described herein provide the ability to achieve a crude tochemical conversion ratio in the range of, for instance, up to 80, 50 or45 wt %, and in certain embodiments in the range of about 39-45 wt %. Incertain embodiments the chemical conversion ratio is at least about 39wt %, and in certain embodiments in the range of about 39-80, 39-50 or,39-45 wt %. It should be appreciated that this crude to chemicalsconversion ratio can vary depending on criteria such as feed, selectedtechnology, catalyst selection and operating conditions for theindividual unit operations.

In some embodiments, individual unit operations can include a controllerto monitor and adjust the product slate as desired. A controller candirect parameters within any of the individual unit operations theapparatus depending upon the desired operating conditions, which may,for example, be based on customer demand and/or market value. Acontroller can adjust or regulate valves, feeders or pumps associatedwith one or more unit operations based upon one or more signalsgenerated by operator data input and/or automatically retrieved data.

Such controllers provide a versatile unit having multiple modes ofoperation, which can respond to multiple inputs to increase theflexibility of the recovered product. The controller can be implementedusing one or more computer systems which can be, for example, ageneral-purpose computer. Alternatively, the computer system can includespecially-programmed, special-purpose hardware, for example, anapplication-specific integrated circuit (ASIC) or controllers intendedfor a particular unit operation within a refinery.

The computer system can include one or more processors typicallyconnected to one or more memory devices, which can comprise, forexample, any one or more of a disk drive memory, a flash memory device,a RAM memory device, or other device for storing data. The memory istypically used for storing programs and data during operation of thesystem. For example, the memory can be used for storing historical datarelating to the parameters over a period of time, as well as operatingdata. Software, including programming code that implements embodimentsof the invention, can be stored on a computer readable and/or writeablenonvolatile recording medium, and then typically copied into memorywherein it can then be executed by one or more processors. Suchprogramming code can be written in any of a plurality of programminglanguages or combinations thereof.

Components of the computer system can be coupled by one or moreinterconnection mechanisms, which can include one or more busses, forinstance, between components that are integrated within a same device,and/or a network, for instance, between components that reside onseparate discrete devices. The interconnection mechanism typicallyenables communications, for instance, data and instructions, to beexchanged between components of the system.

The computer system can also include one or more input devices, forexample, a keyboard, mouse, trackball, microphone, touch screen, andother man-machine interface devices as well as one or more outputdevices, for example, a printing device, display screen, or speaker. Inaddition, the computer system can contain one or more interfaces thatcan connect the computer system to a communication network, in additionor as an alternative to the network that can be formed by one or more ofthe components of the system.

According to one or more embodiments of the processes described herein,the one or more input devices can include sensors and/or flow meters formeasuring any one or more parameters of the apparatus and/or unitoperations thereof. Alternatively, one or more of the sensors, flowmeters, pumps, or other components of the apparatus can be connected toa communication network that is operatively coupled to the computersystem. Any one or more of the above can be coupled to another computersystem or component to communicate with the computer system over one ormore communication networks. Such a configuration permits any sensor orsignal-generating device to be located at a significant distance fromthe computer system and/or allow any sensor to be located at asignificant distance from any subsystem and/or the controller, whilestill providing data therebetween. Such communication mechanisms can beaffected by utilizing any suitable technique including but not limitedto those utilizing wired networks and/or wireless networks andprotocols.

Although the computer system is described above by way of example as onetype of computer system upon which various aspects of the processesherein can be practiced, it should be appreciated that the invention isnot limited to being implemented in software, or on the computer systemas exemplarily described. Indeed, rather than implemented on, forexample, a general purpose computer system, the controller, orcomponents or subsections thereof, can alternatively be implemented as adedicated system or as a dedicated programmable logic controller (PLC)or in a distributed control system. Further, it should be appreciatedthat one or more features or aspects of the processes can be implementedin software, hardware or firmware, or any combination thereof. Forexample, one or more segments of an algorithm executable by a controllercan be performed in separate computers, which in turn, can be incommunication through one or more networks.

In some embodiments, one or more sensors and/or flow meters can beincluded at locations throughout the process, which are in communicationwith a manual operator or an automated control system to implement asuitable process modification in a programmable logic controlledprocess. In one embodiment, a process includes a controller which can beany suitable programmed or dedicated computer system, PLC, ordistributed control system. The flow rates of certain product streamscan be measured, and flow can be redirected as necessary to meet therequisite product slate.

Factors that can result in various adjustments or controls includecustomer demand of the various hydrocarbon products, market value of thevarious hydrocarbon products, feedstock properties such as API gravityor heteroatom content, and product quality (for instance, gasoline andmiddle distillate indicative properties such as octane number forgasoline and cetane number for middle distillates).

The disclosed processes and systems create new outlets for directconversion of crude oil, for instance, light crudes such as Arab ExtraLight (AXL) or Arab Light (AL) crude oil. Additionally, the disclosedprocesses and systems offer novel configurations that, compared to knownprocesses and systems, requires lower capital expenditure relative toconventional approaches of chemical production from fuels or refineryby-products and that utilize refining units and an integrated chemicalscomplex. The disclosed processes and systems substantially increase theproportion of crude oil that is converted to high purity chemicals thattraditionally command high market prices. Complications resulting fromadvancing the threshold of commercially proven process capacities areminimized or eliminated using the processes and systems describedherein.

The disclosed processes and systems utilize different commerciallyproven units arranged in novel configurations. These novelconfigurations enable production of refined products and petrochemicalproducts including olefins, aromatics, MTBE, and butadiene. Thedisclosed processes and systems allow chemicals producers to de-couplefrom fuel markets and have more freedom to increase chemical yields as afraction of crude rate, as compared to traditional chemical productionusing refinery intermediates or by-products as feedstock. Also, thedisclosed processes and systems substantially increase the proportion ofcrude oil that is converted to high purity chemicals that traditionallycommand high market prices.

The disclosed processes and systems provide alternatives for chemicalsproduction that have lower capital investment relative to conventionalroutes that utilize refining units and an integrated chemicals complex.Moreover, the disclosed processes and systems offer the flexibility ofsimultaneously producing fuel products and chemical products. The ratioof chemicals to residual fuels can be modulated by process operations toaddress changing fuels and chemical market opportunities. In certainembodiments, the process configurations are flexible to enableprocessing of crude oil, such as Arab Light or Arab Extra Light, toprovide superior production of chemical products, while minimizing theproduction of refined fuel products. The configurations offer theflexibility to structure operations to adjust the ratio ofpetrochemicals to refined products in order to achieve optimumoperations and allows shifting the production ratio of chemicals tofuels, thereby adjusting to market conditions.

For example, in vacuum gas oil hydroprocessing, as severity increases,the yield of UCO (or hydrotreated gas oil) decreases as the naphthayield increases, although for the most part the distillate yield doeschange as much because wild naphtha product is the result of distillatecracking. The UCO product is chemically restructured through ringopening reactions to become much more paraffinic in nature, and remainsa gas oil boiling range product. By modulating severity of vacuum gasoil hydroprocessing, the shift is between naphtha and UCO (orhydrotreated gas oil) relative product rates. The olefin yield ofnaphtha in the steam cracker is superior to UCO (or hydrotreated gasoil); while the heavy product yield (mixed C4s and pyrolysis gasoline)from UCO (or hydrotreated gas oil) is superior to naphtha. Therefore, akey advantage of modulating the vacuum gas oil hydroprocessingconversion is to economically and dynamically address changing marketconditions for olefin and aromatic products, which may swingdramatically.

Each of the processing units are operated at conditions typical for suchunits, which conditions can be varied based on the type of feed tomaximize, within the capability of the unit's design, the desiredproducts. Desired products can include fractions suitable as feedstockto the mixed feed steam cracking zone 230, or fractions suitable for useas fuel products. Likewise, processing units employ appropriatecatalyst(s) depending upon the feed characteristics and the desiredproducts. Certain embodiments of these operating conditions andcatalysts are described herein, although it shall be appreciated thatvariations are well known in the art and are within the capabilities ofthose skilled in the art.

For the purpose of the simplified schematic illustrations anddescriptions herein, accompanying components that are conventional incrude centers, such as the numerous valves, temperature sensors,preheater(s), desalting operation(s), and the like are not shown.

Further, the numerous valves, temperature sensors, electroniccontrollers and the like that are conventional in fluid catalystcracking are not included. Further, accompanying components that are inconventional in fluid catalyst cracking systems such as, for example,air supplies, catalyst hoppers, flue gas handling the like are also notshown.

In addition, accompanying components that are in conventionalhydroprocessing units such as, for example, hydrogen recyclesub-systems, bleed streams, spent catalyst discharge sub-systems, andcatalyst replacement sub-systems the like are not shown.

Further, accompanying components that are in conventional thermalcracking systems such as steam supplies, coke removal sub-systems,pyrolysis sections, convection sections and the like are not shown.

The method and system of the present invention have been described aboveand in the attached drawings; however, modifications will be apparent tothose of ordinary skill in the art and the scope of protection for theinvention is to be defined by the claims that follow.

The invention claimed is:
 1. An integrated system for producingpetrochemicals and fuel products comprising: an atmospheric distillationunit (ADU) operable to receive and separate a feed, and discharge afirst ADU fraction comprising naphtha, a second ADU fraction comprisingat least a portion of middle distillates from the feed, and a third ADUfraction comprising atmospheric residue; a vacuum distillation unit(VDU) operable to receive and separate the third ADU fraction, anddischarge a first VDU fraction comprising vacuum gas oil; a distillatehydroprocessing (DHP) zone operable to receive and convert middledistillates from the second ADU fraction into a first DHP fraction and asecond DHP fraction, wherein the first DHP fraction comprises naphthaand the second DHP fraction is used for diesel fuel production; acatalytic reforming zone operable to receive and convert naphtha fromthe first ADU fraction into a chemical reformate stream; a fluidcatalytic cracking (FCC) zone operable to receive and convert the firstVDU fraction into a first FCC fraction containing light olefins, asecond FCC fraction containing FCC naphtha and a third FCC fractioncontaining cycle oil; an aromatics extraction zone; a mixed feed steamcracking (MFSC) zone operable to receive and thermally crack a C6-C9non-aromatics raffinate stream derived from the aromatics extractionzone, wherein the steam cracking zone is operable to produce a mixedproduct stream containing mixed C1-C4 paraffins and olefins, a pyrolysisgas stream, and a pyrolysis oil stream; and a naphtha hydroprocessingzone operable to receive and treat the pyrolysis gas stream and producea hydrotreated pyrolysis gas stream; wherein the aromatics extractionzone is operable to receive and separate the hydrotreated pyrolysis gasstream and the chemical reformate stream into one or more aromaticproducts streams, and the C6-C9 non-aromatics raffinate stream.
 2. Thesystem as in claim 1, wherein the catalytic reforming zone includes asemi-regeneration, cyclic regeneration or continuous catalystregeneration arrangement enabling contact of the naphtha feed withmono-functional or bi-functional reforming catalyst, to produce thechemical rich reformate.
 3. The system as in claim 1, further comprisinga naphtha hydrotreating zone operable to receive and treat naphtha fromthe first ADU fraction and produce hydrotreated naphtha stream, andwherein the catalytic reforming zone is operable to receive and convertthe hydrotreated naphtha stream.
 4. The system as in claim 1, furthercomprising a separation zone operable to receive and separate naphthafrom the first ADU fraction into a normal paraffin rich stream and anon-normal paraffin rich stream containing branched paraffins, whereinthe catalytic reforming zone is operable to receive and treat thenon-normal paraffin rich stream and wherein the MFSC zone is operable toreceive and thermally crack the normal paraffin rich stream.
 5. Thesystem as in claim 1, further comprising an FCC naphtha hydrotreatingzone operable to receive and treat naphtha from the second FCC fractionand produce a hydrotreated FCC naphtha fraction.
 6. The system as inclaim 5, wherein the FCC naphtha hydrotreating zone is operable toseparate C5s from hydrotreated FCC naphtha fraction, and wherein theMFSC zone is operable to receive C5s separated from hydrotreated FCCnaphtha fraction.
 7. The system as in claim 5, wherein the aromaticsextraction zone is operable to receive and separate aromatics from thehydrotreated FCC naphtha fraction.
 8. The system as in claim 1, furthercomprising a gas oil hydroprocessing (GOHP) zone operable to receive andtreat vacuum gas oil from the first VDU fraction and produce a firstGOHP fraction containing naphtha range components, and a second GOHPfraction containing heavy oil, which is hydrotreated gas oil orunconverted oil in the vacuum gas oil range, and wherein the FCC zone isoperable to receive the second GOHP fraction.
 9. The system as in claim8, wherein the MFSC zone is operable to receive and thermally cracknaphtha from the first DHP fraction, naphtha from the first GOHPfraction, or both naphtha from the first DHP fraction and naphtha fromthe GOHP fraction.
 10. The system as in claim 1, wherein the naphthahydrotreating zone is operable to produce a C5s stream, and wherein theMFSC zone is operable to receive and thermally crack the C5s stream. 11.The system as in claim 8, wherein the ADU is further operable to receiveand separate naphtha from the first DHP fraction, naphtha from the GOHPfraction, or both naphtha from the first DHP fraction and naphtha fromthe GOHP fraction.
 12. The system as in claim 1, wherein the ADU isoperable to separate a further ADU fraction including kerosene that isheavier than the first ADU fraction and lighter than the second ADUfraction, and the system further comprising a kerosene sweetening zoneoperable to receive and treat the further ADU fraction.
 13. The systemas in claim 12, wherein the ADU is operable to separate a further ADUfraction including heavy AGO that is heavier than the second ADUfraction and lighter than the third ADU fraction, and wherein (a) theFCC zone is operable to receive and thermally crack the additional ADUfraction, or (b) the GOHP zone is operable to receive and convert theadditional ADU fraction.
 14. The system as in claim 1, furthercomprising: an olefins recovery train operable to receive and separatethe mixed product into a fuel gas stream, an ethylene stream, a mixedC3s stream, and a mixed C4s stream, and a C4 distillation unit operableto receive and separate a portion of C4s recovered from the mixedproduct stream into an olefinic stream and a non-olefinic stream. 15.The system as in claim 14, wherein the MFSC zone is operable to receiveand thermally crack the non-olefinic stream.
 16. The system as in claim14, further comprising a mixed butanols production zone operable toreceive and convert a mixture of butenes from the C4 distillation unitinto a mixed butanol product stream.
 17. The system as in claim 14,further comprising a metathesis reaction zone operable to receive andconvert all or a portion of the C5s stream into a propylene stream, anda C4/C5 raffinate stream, and wherein the MFSC zone is operable toreceive and thermally crack the C4/C5 raffinate stream.
 18. The systemas in claim 14, wherein the FCC naphtha hydrotreating zone is operableto separate C5s from hydrotreated FCC naphtha fraction prior toseparation of aromatics in the aromatics extraction zone, or the naphthahydrotreating zone is operable to produce a C5s stream; and furthercomprising a metathesis reaction zone operable to receive and convertall or a portion of the C5s stream into a propylene stream, and a C4/C5raffinate stream; and a mixed butanols production zone operable toreceive and convert a mixture of butenes from the C4 distillation unitinto a mixed butanol product stream and an alkanes stream; wherein theMFSC zone is operable to receive and thermally crack the non-olefinicstream and the C4/C5 raffinate stream.
 19. The system as in claim 1,further comprising the distillate hydroprocessing (DHP) zone is operableto receive the third FCC fraction containing cycle oil.
 20. The systemas in claim 6, wherein the aromatics extraction zone is operable toreceive and separate aromatics from the hydrotreated FCC naphthafraction having C5s removed.